Corken Specialty Selection Guide Selective Catalytic ... · PDF fileCorken Specialty Selection Guide Selective Catalytic Reduction Systems • Anhydrous Ammonia • Aqueous Ammonia

Corken SpecialtySelection Guide

SelectiveCatalyticReductionSystems

• Anhydrous Ammonia

• Aqueous Ammonia

• Urea

Corken, a tradition of excellence

As a unit of IDEX Corporation, Corken Inc. is a leader in

specialized niche markets. To maintain our leadership in your

industry requires continual Innovation, Diversity and Excellence.

With over 50 years of global experience in liquefied gas handling,

Corken offers unparalleled experience in rapidly changing ammonia

handling systems. Corken’s exceptional reputation is built upon

decades of maintaining the highest quality and customer service

standards. Corken follows all of the guidelines set out by national

agencies like the American National Standard Institute (ANSI) and

the American Society of Mechanical Engineers (ASME) as they

apply to our products.

Through intimate contact within your industry, Corken is

committed to applying new product technology and streamlining

product selection.

This specialized information packet is designed as a

comprehensive guide to applying Corken products in your

industry. It covers the capabilities, applications and guidelines for

use of our compressors and pumps specifically for NH3 transfer in

selective catalyst reduction (SCR) systems.

SCR Definition and OverviewSelective Catalytic Reduction (SCR): a post-combustion NOX reduction technology in which ammonia (NH3) isadded to the flue gas, which then passes through layers of a catalyst. The ammonia and NOX react on the surface ofthe catalyst, forming harmless nitrogen (N2) and water vapor.

New Environmental Protection Agency (EPA) regulations generate high demand for SCR systems to reduce NOX

emissions from many large fossil-fuel fired industrial boilers and electricity generating units. The emerging demandfor SCR systems also creates market opportunities for Corken equipment. SCR systems can reduce NOX levels by90% or more. The SCR market is mainly driven by environmental regulations and environmental technologies.

SCR is well accepted by the industry as the best available technology, achieving the highest NOX reductionlevel. Technologies are changing rapidly in the NOX reduction SCR market and new alternative technologieskeep coming to the market. Ammonia is currently considered the most effective NOX reducing agent used withSCR systems. Ammonia-based SCR systems can use three different NOX reducing agents: anhydrous ammonia,aqueous ammonia, and urea.

ANHYDROUS AMMONIA TECHNOLOGY• Anhydrous ammonia is the most effective NOX reducing agent used in SCR systems. However, due to its

hazardous nature, this form of ammonia can incur high compliance costs and safety concerns related totransportation, storing, and handling.

• This technology has been in use in Europe since the 1980’s. • Corken pumps and compressors are used in anhydrous ammonia SCR systems.

AQUEOUS AMMONIA TECHNOLOGY• Aqueous ammonia is commonly used in concentrations of 19% and 29% in SCR systems. When diluted to 19%

concentration, aqueous ammonia is not classified as a toxic chemical. • Aqueous ammonia is generally considered safer than anhydrous ammonia because of its lower toxicity and lower

storage pressure. • Corken pumps are used as feed pumps in aqueous ammonia systems.

UREA BASED AMMONIA GENERATION TECHNOLOGY• Non-toxic urea is transported as a granular solid. It is mixed with water on site and converted to ammonia to be

used as a NOX reducing agent in SCR systems.• This technology has recently gained a lot of interest from end-users due to minimal safety concerns. This

technology is in the growth stage of its product life cycle. • Corken pumps are used in urea based SCR systems.

CoalAir

Ash

Boiler

EconomizerBypass

AmmoniaInjection

SCRReactor

AirPreaheater

ElectrostaticPrecipitator

Ash

Stack

To Disposal

Where is Corken Equipment Applied inSCR Systems?

NH3 Storage

NH3 Railcar

Corken feed pump foranhydrous ammonia,aqueous ammonia,urea solution

Coal-fired power plantusing SCR system

Corken unloadingcompressor foranhydrous ammonia

Wide Ranging Flows and PressuresCorken offers specialized pumping technologies where flows range from 1-400 gpm with differential pressuresto 1,100 feet.

Low Net Positive Suction Head (NPSH)No need to compromise system design or experience down time associated with vapor lock and cavitation.Corken’s unique design exceeds expectations where NPSH is as low as 1 ft.

Continuous Duty ServiceCorken offers a continuous rated design. Reduced operating speed and free-floating impellers (no metal-to-metal contact) provide years of trouble free service.

Sealing IntegrityWhether your application calls for mechanical sealing or sealless designs, Corken provides the widest range of options.

Commitment and SupportCorken products are backed by the strongest service commitment in your industry. We are pleased to provideyou with our growing list of satisfied customers.

Corken Industrial Pumps andCompressors Meet the Challenges ofSCR Ammonia Transfer

Proven ReliabilityCorken Industrial Compressors have been the standard in bulk ammonia transfer for 50 years. Our product andsystem experience in ammonia handling allows us to streamline your selection process.

Sealing / Environmental ControlCorken’s proven double distance piece (t-style) offering is specifically designed for hazardous gases. OptionalANSI/DIN flanges provide increased environmental security.

One Stop ShoppingCorken compressor packages are engineered to customer specifications. No other company offers the rangeof Selective Catalytic Reduction (SCR) ammonia pump and compressor system capability.

COMPRESSORS FOR ANHYDROUS AMMONIA

PUMPS FOR ANHYDROUS AMMONIA, AQUEOUS AMMONIAAND UREA

All Contents Copyright © 2000 Corken, Inc., a Unit of IDEX Corporation.3805 N.W. 36th St., Oklahoma City, OK 73112

WHY USE A COMPRESSOR TO TRANSFER HIGHLY VOLATILE LIQUIDS? . . . . . . . . . . . . . . . . . . 8GUIDE TO COMPRESSOR SELECTION . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 9

Specifications. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 11Choose From a Variety of Mounting Arrangements to Suit Your Particular Application . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 11Outline Dimensions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 12Material Specifications. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 15The Transfer Compressor Operating Principle . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 16Economics of Using a Compressor . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 17Simplified Bulk Plant Piping Details . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 18Typical Transport Mounting Arrangement . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 18Ammonia Compressor Selection Table . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 19Moving Liquid with Vapor . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 20Liquid Transfer and Vapor Recovery. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 22Liquefied Gas Transfer Compressor Worksheets. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 23Compressor Foundation Design . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25

GUIDE TO PUMP SELECTION . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 28SC-Series Side Channel Pumps . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 29Principle of Side Channel Operation. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 30Selection Overview Graphs . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 31Instructions for Selection of Mechanical Seal Model . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 33Instructions for Selection of Magnetic Drive Model . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 34Magnetic Coupling Selection Table . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 35Performance Curves . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 36Material Specifications. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 48Model Number Selection Guide for Mechanical Seal Model . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 49Model Number Selection Guide for Magnetic Drive Model . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 50Dimensional Drawings . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 51Piping Recommendations . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 53The Corken B166 Bypass Valve . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 60The Corken T166 Bypass Valve . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 61

WARRANTY INFORMATION . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 62

CONVERSION FACTORS. . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 63

PRODUCT APPLICATION FORM . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 64

A Comprehensive Guide to SCR Systems

8

Why Use a Compressor to Transfer Highly Volatile Liquids?

Liquefied gases must be transferred from one container to anothereither with a liquid pump or a gas compressor, and there are verydefinite benefits from selecting either one. Because Corken has hadmany years of experience in manufacturing both pumps andcompressors for volatile liquid service, it is possible for ourpersonnel to analyze this problem objectively and present thefollowing comparisons to assist you in making the proper choice.

LIQUID PUMPS

A liquid pump, such as the Corken Coro-Vane® has the advantage ofproducing higher differential pressures than the compressor toovercome high pressure losses caused by inadequate discharge piping,pumping into small, hard to fill tanks, and particularly through meters.A compressor cannot successfully discharge volatile liquid through ameter. However, the liquid pump does have certain limitations:

• Volatile liquids with their tendency to boil or "flash" readilywhenever the pressure is reduced require particular attention topump installation.

• To reduce this "flashing" effect, pump inlet piping-must bedesigned carefully with larger and more expensive valves,strainers and flexible piping arrangements to provide the pump'srequired NPSH (net positive suction head).

• Most tank cars have top outlets, necessitating a "siphon leg" whichcontributes to liquid flashing.

• The flashing liquid may cause pump "vapor lock", with theattendant loss of capacity and accelerated wear on the shaft sealsand running parts.

• Tanks are seldom emptied entirely of liquid; uneven unloading sitesand variations in the vehicle undercarriage increase this possibility.

None of the valuable residual vapors remaining in the unloaded tankmay be recovered.

GAS COMPRESSORS

A gas compressor will overcome many of the obstacles associatedwith transferring liquid with a pump, such as poor piping conditionsand top outlet tanks. The compressor will do everything the pumpwill do in low pressure liquid transfer, with the same horsepowerrequirement, and will recover the valuable residual vapors. Thequantities of recoverable residual vapors are shown in Figure 1, page16 for typical gases.

Transports have bottom openings and may be unloaded with a liquidpump successfully. The amount of valuable vapors remaining usuallyis not as great as in a tank car, and a transporter understandably isreluctant to leave his expensive equipment for an hour or so whilethe residual vapors are being recovered. Because of these factors,many "transport only" bulk plants utilize only liquid pumps. Yet it isreasonable to expect that the plant operator could recover vapors forthe period of time the driver is performing his accounting chores, ifa plant compressor were available. Figure 1, page 17, illustrates thata large percentage of the vapors may be recovered in the first 15 to30 minutes. Actually, more equivalent pounds or gallons of vaporwill be recovered during the first few minutes while the residualliquid is being vaporized than will be reclaimed during the sameperiod of time later on. The vaporized liquid content is in addition tothe values shown in Figure 1, page 17.

Even when gas ownership does not change hands, as in the case whena producer delivers to his own terminal, the vapor recoverycompressor can develop an increased transporting capacity of about3 percent! This means a fleet of 97 tank cars unloaded with vaporrecovery can do the job of 100 when the vapor is not recovered!

Maintenance of a pump or a compressor is about the same if theequipment is not abused. The liquid pump can be damaged seriouslyif allowed to run dry, either from "vapor locking" or after theunloading tank is emptied, whereas the compressor is remarkablyresistant to this kind of abuse. You must, however, take action toprevent liquid entering the compressor.

Safety of plant operation is a factor often not considered incompressor selection: a safety minded operator will use the versatilecompressor to evacuate tanks and piping rather than "bleedingdown". He will also find the purging of new tanks is more effectivelydone by first evacuating the air with the compressor.

Today, in the gas distribution business with the price of productincreasing and competition more pressing, profits are more difficultto produce than ever before. The profit contribution of vaporrecovery may very well make the difference in an acceptable profitmargin; the discussion on the "Economics of Compressor Operation"indicates this clearly, and is a logical method you may use to justifyyour own decision.

Profits will continue to accrue whenever vapor recovery operationsare performed.

9

10

FEATURES

ANSI FLANGED HEAD is made from ductile iron and is ideal formost industrial applications. ANSI flanges eliminate the possibilityof leaks from threaded connections.

PISTON ROD SEALS of glass-filled, self-lubricating Teflon® arespring loaded and adjustable to compensate for lateral rodmovement, wear and temperature variations. The seals stop gasleakage into the crankcase and crankcase oil entry into thecompression cylinders.

CROSSHEAD – PISTON ROD assemblies transmit the crankshaftmotion into vertical, reciprocating piston motion. The vertical pistonmotion provides no side thrust, and thus the pistons require no riderrings. The crosshead and the hardened steel piston rod are assembledand machined as one piece to assure perfect alignment between theconnecting rod wrist pin and the piston rod.

CRANKSHAFTS have integral, balanced counterweights for smootheroperation. Bearing surfaces are extra large and the crankshaft isprecision ground to size. The crankshafts are rifle drilled for positiveoil distribution to the connecting rods and wrist pin bearings.

THE CRANKCASE is operated at atmospheric pressure, but istotally enclosed with an automatic breather valve to prevent entranceof dust or foreign matter. Since no oil is consumed in thecompression process, the oil remains clean in the crankcase, and themajor sources of crankcase wear are virtually eliminated. The oilstays in the crankcase where it belongs! The crankshaft runningparts are pressure lubricated by filtered oil from an automaticallyreversible pump (reversing does not require disassembly). An easy-to-read, dial-type, oil pressure gauge indicates proper functioning ofthe lubrication system.

TAPERED ROLLER BEARINGS are mounted on each end of thecrankshaft to absorb radial and thrust loads. These oversize bearingsassure added years of service, and can be adjusted easily from theexternal position of the crankcase if required.

CUSHIONED VALVES are designed and lapped for long life. Thevalve bumpers have a gas cushion to prevent valve slamming andprovide quiet operation. Each valve is easily removable for inspection.

OIL-FREE CYLINDER AND PISTON DESIGN permits thesecompressors to operate with no lubrication of any kind in thecompression cylinders. A combination of self-lubricating, filled

Teflon® piston rings, honed cylinder walls and low lift valves makethis unique pumping system possible. The pistons are arranged notto contact the cylinder wall and are designed to be removable fromthe cylinder and piston rod without disturbing the cylinder.

INTERNAL PROTECTION DEVICES guard against liquid slugging.Volatile liquid transfer incurs risk of liquid entering or "slugging" thecompressor. Reliable relieving devices are built into the cylinder headand suction valves to prevent damage from reasonable amounts ofliquid. An optional liquid trap provides additional protectionexternally, and is recommended for all plant installations.

LARGE FLYWHEEL FAN provides maximum crankcase coolingand smooth operation.

DUCTILE IRON CONNECTING RODS provide great strength forheavy duty applications. The connecting rod bearing inserts aresteel backed, babbit-lined, removable automotive type. The rod isconstructed with a communicating lubrication port from the crankto the honed bronze wrist pin bearing for lubrication from thecrankcase oil pump.

Teflon® is a registered trademark of DuPont.

Guide to Compressor Selection1

FD491 COMPRESSOR

NOTES:1. The driver horsepower shown is based upon recovering residual vapors in moderate climates.2. The actual capacity will vary depending upon piping factors. The capacities shown are conservative and may be increased as

much as 10% in well designed plants.

There are a number of standard base mounted gas compressor units tofit most installations, but special mounting and piping arrangementscan be designed and manufactured to fit your particular needs.

BAREGas compressor with flywheel.

STYLE – 103Gas compressor unit with pressure gauges, steel baseplate,adjustable driver slide base, v-belt drive and enclosed belt guard –ready to receive an electric motor driver.

STYLE – 107FComplete gas compressor bulk plant unit with ANSI flangedmounting includes pressure gauges / block valves, ASME code

stamped ANSI flange inlet trap with one or two liquid levelswitches, flanged trap relief valve, manual tank drain, non-lubeANSI flanged four-way valve and flange welded interconnectingpiping. Mounted on a steel base, v-belt drive and enclosed beltguard. Motor and flanged compressor not included.

Style – 109FGas compressor unit with ANSI flanged mounting includes pressuregauges / block valves, ASME code stamped ANSI flange inlet trapwith two liquid level switches, flanged trap relief valve and manualtank drain and flange welded interconnecting piping. Mounted on asteel base, v-belt drive and enclosed belt guard. Motor and flangedcompressor not included.

CHOOSE FROM A VARIETY OF MOUNTING ARRANGEMENTS TO SUIT YOUR PARTICULAR APPLICATION

COMPRESSOR SELECTION CHART

11

MODEL SIZESPECIFICATION FD291 FD491 FD691Number of Stages 1 1 1Number of Cylinders 2 2 2Bore of Cylinder, inches (cm) 3 (7.62) 4 (10.16) 4.5 (11.43)Stroke, inches (cm) 2.5 (6.35) 3 (7.62) 4 (10.16)Piston Displacement, cfm (m2/hr)

Minimum at 400 rpm 8 (18.6) 17 (28.9) 29 (49.3)Maximum at 825 rpm 16 (27.2) 36 (61.2) 60 (102)

Maximum Discharge Pressure, psig (bars g) 335 (23.1) 335 (23.1) 335 (23.1)Maximum Compression Ratio: Continuous Duty 5 5 5

Intermittent Duty 7 7 7Maximum Allowable Driver Size, hp 15 20 30

MOTOR APPROXIMATE CAPACITYCOMPRESSOR SIZE, FOR AMMONIA

MODEL HORSEPOWER1 GPM (LIT/MIN)2

3 44 (166)291 5 77 (291)

7-1/2 88 (333)5 77 (291)

491 7-1/2 110 (416)10 148 (560)15 198 (749)10 132 (500)

691 15 198 (749)20 265 (1,003)25 330 (1,249)

MECHANICAL SPECIFICATIONS

SPECIFICATIONS

Guide to Compressor Selection 1

5-1/4(13.34)

10-1/8(25.64)

1-1/2 (3.81)

2-13/16 (7.14)

BELTGUARD

HIGH LIQUID LEVELSHUTDOWN SWITCH1-1/2" 300 LB R.F.ANSI FLANGE

1/2" NPTCRANKCASEOIL DRAIN

FOUR WAYCONTROL VALVE

3/4" 300 LBR.F. FLANGE

INLET PRESSURE

GAUGE

LIQUID TRAP

CRANKCASEHEATER

(OPTIONAL)

NEMA 7 LOW OILPRESSURE SWITCH

(OPTIONAL)

ADJUSTABLEDRIVER

SLIDE BASE

USE EIGHT1/2" ANCHOR

BOLTS

ELECTRIC MOTORDRIVER

PIPETAP

MERCER RELIEF VALVE1" 300# X 2" 150# ANSIFLANGE PIPE-AWAYSET AT 350 PSIG

HIGH TEMPERATURESHUTDOWN SWITCH

(OPTIONAL)

DISCHARGEPRESSURE

GAUGE

1" 300 LB. R.F. FLANGERELIEF VALVE TO BE

CUSTOMER SUPPLIED

UNLOADERS(OPTIONAL)

SUCTION VALVE

4 1/2(11.43)

0 321010 20 30 40

ALL DIMENSIONS IN INCHES(CM)

20 (50.80)

14-1/8 (35.88)

49-13/16(126.53)

44-3/16(112.24)

18-1/2 (46.99)

34-1/2(87.60)

28-1/4(71.79)

19-3/8(49.21)

6-7/8(17.46)

4(10.16)

DRAIN VALVE1" 300 LB R.F.ANSI FLANGE

1-1/4 (3.17)15-1/2 (39.45)

21 (53.34)

21-5/16 (54.13)47 (119.38)

66-3/4 (169.55)68 (172.72)

OU

TLIN

E D

IMEN

SIO

NS

– FD

291-1

07F

Gui

de to

Com

pres

sor S

elec

tion

1

12

1302

0 321PSI

KG/CM‹

0 10 20 30 40

68 (172.72)

4(10.16)

10-5/16(26.21)

22-13/16(57.96)

31-5/16(79.46)

38-3/8(97.41)

47-5/8(120.98)

53-1/4(135.27)

1-1/4 (3.17)13-13/16 (35.16)

18-5/16 (46.51)21 (53.34)

47 (119.38)66-3/4 (169.55)

11-3/4(29.80)

1-1/2 (3.81)1-9/16 (3.97)

12-7/8 (32.66)18-1/2 (46.99)20 (50.80)

4-1/2(114.3)

FOUR WAYCONTROL VALVE

1-1/4" 300 LBR.F. FLANGE

5-1/4(13.34)

INLETPRESSURE GAUGE

BELTGUARD

NEMA 7 LOW OILPRESSURE SWITCH

(OPTIONAL)

LIQUID TRAP

HIGH LIQUIDLEVEL SHUTDOWNSWITCH 1-1/2"300 LB R.F.ANSI FLANGE

MERCER RELIEF VALVE1" 300# x 2" 150# ANSIFLANGE PIPE-AWAYSET AT 350 PSIG

ELECTRIC MOTORDRIVER

PIPETAP

ADJUSTABLEDRIVER

SLIDE BASE

USE EIGHT1/2" ANCHOR

BOLTS

CRANKCASEHEATER

(OPTIONAL)

DRAIN VALVE1" 300 LB R.F.ANSI FLANGE

1/2" NPTCRANK CASEOIL DRAIN

HIGH TEMPERATURESHUTDOWN SWITCH(OPTIONAL)

DISCHARGEPRESSURE GAUGE

1" 300 LB R.F. FLANGERELIEF VALVE TO BE

CUSTOMER SUPPLIED

ALL DIMENSIONS IN INCHES(CM)

SUCTION VALVEUNLOADERS (OPTIONAL)

13

OU

TLINE D

IMEN

SION

S – FD491-1

07F

Guide to Com

pressor Selection1

0 321

0 10 20 30 40

1/2" NPTCRANKCASE DRAIN

INLETPRESSURE

GAUGE(OPTIONAL)

DISCHARGEPRESSUREGAUGE(OPTIONAL)

DISCHARGETEMPERATURE

GAUGE(OPTIONAL)

THREE-WAY SOLENOIDUNLOADER VALVE

(OPTIONAL)

LIQUID TRAP

BELTGUARD

HIGH LIQUID LEVELSHUTDOWN SWITCH1-1/2" 300 LB R.F.ANSI FLANGE

HIGH LIQUID LEVELALARM SWITCH1-1/2" 300 LB R.F.ANSI FLANGE

ELECTRICMOTORDRIVER

PIPETAP

CRANKCASEHEATER

(OPTIONAL) ADJUSTABLEDRIVER

SLIDE BASEUSE EIGHT

3/4"ANCHORBOLTS

NEMA 7 LOWOIL PRESSURE

SWITCH(OPTIONAL)

DRAIN VALVE1-1/2" 300 LB R.F.ANSI FLANGE

FOURWAY

CONTROLVALVE 2"

300 LBR.F. FLANGE

DISCHARGEPRESSURE GAUGE

SUCTION VALVEUNLOADERS(OPTIONAL)

HIGH TEMPERATURESHUTDOWN SWITCH

(OPTIONAL)

1" 300 LB R.F.FLANGE RELIEF VALVECUSTOMER SUPPLIED

INLETPRESSURE

GAUGE

MERCER RELIEF VALVE1" 300# x 2" 150# ANSIFLANGE PIPE-AWAY

SET AT 350 PSIG

15-3/16(38.50)

5-1/2(13.97)

14-1/4 (36.20)3/4 (1.91)

23-1/4 (59.06)24 (60.96)

1/8 (0.40)

9 (22.86)9-3/8 (23.80)

27 (68.58)39-1/4 (99.70)

45 (114.30)63 (160.02)

1-3/8 (3.48)

72 (182.88)

85-1/8(216.30)

4-1/2 (11.43)

79-1/2(202.01)

35(88.90)

28-1/2(72.39)

10-1/2(26.67) 6

(15.24)

8-3/4(22.23)

54-7/8(139.36)

53-1/8(134.99)

36-5/8(93.01)

DIMENSIONS IN INCHES (CM)

14

OU

TLIN

E D

IMEN

SIO

NS

- FD

691-1

07F

Gui

de to

Com

pres

sor S

elec

tion

1

15

STANDARD OPTIONAL

PART SIZE MATERIAL SIZE MATERIAL

HEAD, CYLINDER91, 191, 291,

DUCTILE IRON ASTM A536 492-692DUCTILE IRON

491, 691 DIN 1693 666-40.3

DISTANCE PIECE,

CROSSHEAD GUIDEALL GRAY IRON ASTM A48, CLASS 30

CRANKCASE, FLYWHEEL

BEARING CARRIER

FLANGE 691 DUCTILE IRON ASTM A536 690, 691, 690-4 STEEL WELDING

291 17-4 PH STAINLESS STEEL

VALVE SEAT AND BUMPER 391, 491, 491-3 DUCTILE IRON ASTM A536

691 STAINLESS STEEL

291 410 STAINLESS STEEL 291 PEEK

VALVE PLATE 491, 491-3 17-7 PH STAINLESS STEEL

691 STAINLESS STEEL 691 PEEK

VALVE SPRING291, 691 17-7 STAINLESS STEEL

491, 491-3 INCONEL

VALVE GASKETS ALL SOFT ALUMINUM ALL COPPER, IRON-LEAD

PISTON 291, 491, 691 GRAY IRON ASTM A48, CLASS 30

PISTON ROD ALLC1050 STEEL, NITROTEC, ALL D & T STYLE

CHROME OXIDE COATINGROCKWELL 60C MODELS

CROSSHEAD ALL GRAY IRON ASTM A48, CLASS 30

PISTON RINGS ALL PTFE, GLASS AND MOLY FILLED ALL SPECIAL ORDER

OR ALLOY 50 MATERIALS AVAILABLE

PISTON RING EXPANDERS ALL 302 STAINLESS STEEL NONE

HEAD GASKET 291, 491, 691 O-RING (BUNA-N) 291, 491, 691 PTFE, VITON®, NEOPRENE®

ADAPTER PLATE,

PACKING CARTRIDGE, ALL DUCTILE IRON ASTM A536

CONNECTING ROD

PACKING RINGS ALLPTFE, GLASS AND MOLY FILLED SPECIAL ORDER

OR ALLOY 50 MATERIALS AVAILABLE

CRANKSHAFT ALL DUCTILE IRON ASTM A536

CONNECTING ROD BEARING ALL BIMETAL D-2 BABBIT

WRIST PIN ALL C1018 STEEL, ROCKWELL 62C

WRIST PIN BUSHING ALL BRONZE SAE 660

MAIN BEARING ALL TAPERED ROLLER

INSPECTION PLATE ALL ALUMINUM

O-RINGS ALL BUNA-N ALL PTFE, VITON®, NEOPRENE®

RETAINER RINGS ALL STEEL

MISCELLANEOUS GASKETS ALL COROPRENE

VITON® AND NEOPRENE® ARE REGISTERED TRADEMARKS OF DUPONT.

MATERIAL SPECIFICATIONS


THE TRANSFER COMPRESSOR OPERATING PRINCIPLE


16

Most people are somewhat familiar with the operating principles ofa liquid pump; the transfer compressor is another matter entirely.Visualize a tank car full of volatile liquid on a plant siding ready tobe unloaded into storage tanks. Both tank car and storage tank arenormally under approximately the same vapor pressure.

A piping connection is made between the tops of vapor sections of thetank car and the storage tank, and a similar connection is made betweenthe liquid sections of the two tanks. As the connections are opened, theliquid will seek its own level and then flow will stop. However, bycreating pressure in the tank car sufficient to overcome pipe friction andany static elevation difference between the tanks, all the liquid is forcedinto the storage tank quickly. The gas compressor does this job bydrawing gas from the top of the storage tank. This procedure lowers thestorage tank pressure slightly and increases the tank car pressure,

normally 10 to 20 psig (0.7 to 1.4 bars), above vapor pressure.After all possible liquid has been transferred in this manner, someliquid still remains, and the tank car is still full of valuable vapors.To remove the remaining liquid and the residual vapors, pipingconnections are reversed by means of the compressor four-waycontrol valve, and the direction of flow through the compressor isreversed. After closing the connection between the liquid sections ofthe two tanks, the gas can now be drawn from the top of the tank carthereby vaporizing the remaining liquid. After all liquid has beenvaporized, the compressor continues to draw gas from the tank caruntil the tank car pressure is reduced to an economical point.

The recovered vapors must be discharged into the storage tank liquidsection where they will be condensed. If the recovered vapors are notcondensed, the storage tank will develop an excessive pressure.

Vapor Recovery Line

Any claim of an equipment manufacturer should be supported by facts,including the economics or payout calculations. If the profitability ofa piece of machinery cannot be proven, it probably should not bepurchased. The "proof of profit" of an unloading compressor is quitesimple, if certain conservative assumptions are agreed upon:

1 . Either a liquid pump or a compressor must be used to transferthe liquid product.

2. The liquid transfer capacity of either a pump or a compressor,horsepower for horsepower, is comparable. In the Corken line, agas compressor requires the same horsepower for liquid transferonly as does a liquid pump.

3. Since a transfer compressor may recover residual vapors, and aliquid pump cannot, it is to be expected that the horsepowerrequirements for this cycle of operation are greater for a compressor.

4. Only the difference in cost between the compressor and its motorand that of a pump and its motor is to be considered in the payoutsince one or the other must be utilized to transfer the liquid.

5. The cost of operation of the compressor for the vapor recoverycycle is offset by the recovery of the vaporized liquid left in thetank after the transfer of all possible liquid is completed.

Example A:How many tank cars of propane, 33,000 wg capacity, must be unloadedof vapor to pay for a $4,940 compressor? For the sake of simplicity, weshall be unloading cars with an average pressure of 125 psig, and aproduct cost, including freight, of $0.52 per gallon. A liquid pump ofcomparable capacity costs approximately $1,525. The recoverable vaporsin equivalent gallons of liquid are shown in Figure 1 as 770 gallons.

Number of Tank Cars = $4,940-$1,525 = 8770 gal. x $0.52/gal.

Only eight tank cars to pay for a 15 hp compressor unit ... thereafterall vapors recovered are profit!!!

Example B:How many tank cars of ammonia, 11000 wg capacity, must beunloaded of vapor to pay for a 90 gpm, 5 hp compressor, if the tankcar pressures are approximately 150 psig, and the product value is$225 per ton, or $0.113 per pound? A 2-1/2” liquid pump of the samehorsepower would remove the liquid as quickly as the compressor. Theapproximate difference in cost between the compressor and pump is$2,860. Figure 1 shows 1,490 equivalent lbs. of vapor remaining in a33,000 wg car; since our example tank car is only 11,000 wg, theremaining equivalent vapor is approximately 500 lbs.

Number of Tank Cars = $2,860 = 50500 lbs. x $0.113

TANK CAR PRESSURE GALLONS (LITERS) POUNDS (KILOGRAMS)PSIG (BARS)1 OF LP GAS2 OF AMMONIA2

200 (13.79) –– 2,090 (948)175 (12.06) 1,170 (4428) 1,790 (812)150 (10.34) 970 (3671) 1,490 (676)125 (8.61) 770 (2914) 1,190 (540)100 (6.90) 570 (2157) 890 (404)75 (5.17) 370 (1400) 590 (268)50 (3.45) 170 (643) 290 (132)

TIME - HOURS

TAN

K C

AR

PR

ES

SU

RE

BA

RS

PS

IG

0 1 2 3 4 500

123456789

10

25

50

75

100

125

150

NOTES:1. This pressure is that of the tank car before vapor recovery

operations are begun. Capacities are based upon recoveringvapors to 25 psig (1.72 bars).

2. There are several different tank car and transport tankcapacities. When the unloading tank is of different capacitythan 33,000 gallons, the liquid recovery capacities shownhere will be proportional. For example, if the tank car is only11,000 water gallon capacity, the values shown here will bemultiplied by 11,000 ÷ 33,000, or one third.

NOTES:1. Economic recovery time is about three hours. More than half

of economically recoverable vapor is removed in the first hour.2. Vapor recovery is economic to about 25 percent of

storage tank pressure.3. Curve is based on the use of a 36 cfm (1,020 lit/min)

displacement Corken dry-cylinder model 491compressor recovering vapor through 1-1/2" vaporpiping into 150 psig (10.34 bars) storage tank pressure.

VAPOR LEFT IN A 33,000 WATER GALLON(124,905 LITER) CAPACITY TANK CAR

EXPRESSED IN LIQUID CAPACITY

PROPANE EVACUATION TIME FOR 33,000WATER GALLON (124,905 LITER) CAPACITY

TANK CAR

FIGURE 1

17

ECONOMICS OF USING A COMPRESSOR


18

SIMPLIFIED BULK PLANT PIPING DETAILS


DIRECT DRIVE MOUNTING: The compressor is hung inside themain truck frame in line with the PTO. Power is transmitted througha U-joint drive shaft directly to the compressor. Use extendedcrankshaft compressor models.

BELT DRIVE MOUNTING: The location of the fifth wheel anddesign of the tanks determine whether the compressor can bemounted behind the cab, above the frame, or outside the frame.

TYPICAL TRANSPORT MOUNTING ARRANGEMENT

Many companies increase their operating efficiency by equipping their transports with Corken compressors, enabling them to handle a greater varietyof liquids with complete independence from the pumping facilities at the destination. The increased time savings in unloading pays for the compressor.Corken compressors often are mounted behind the tractor cab for direct drive from the truck power take off (PTO) or through a V-belt arrangement.

An engine driven compressor is used whenever it is impractical to use the truck engine, and it may be mounted anywhere on the cab or tanker.

Installation piping details are available for the arrangement shown here or for larger and more complex operations.

SERVICE VALVESTO PERFORM FOUR-WAY A B C1. Unload into Position Open Open Close

Storage Tank One2. Recover Vapors Position Close Open Open

into Storage Tank Two3. Load Out from Position Open Open Close

Storage Tank Two

Vapor line to vaporsection of storage

Vapor line to liquid phasefor vapor recovery

Relief valve

Check valve

Four-wayvalve

AC

BVapor line to loadingand unloading risers

PositionOne

PositionTwo

A C

B

Four-wayvalve

FIGURE 2

19

Consult factory for compressors for higher flows.NOTES: 1. The capacities shown are based on 70°F, but will vary depending upon piping, fittings used, product being transferred and temperature.

The factory can supply a detailed computer analysis if required.2. Driver sheaves: 291, 491 - three belts; 691 - four belts3. The piping sizes shown are considered minimum. If the length exceeds 100 ft., use the next larger size.

DRIVER HORSEPOWERLIQUID LIQUID

TRANSFER TRANSFERAND WITHOUT

DRIVER SHEAVE RESIDUAL RESIDUALSIZE P.D. (2) VAPOR VAPOR PIPING SIZE

CAPACITY DISPLACEMENT COMPRESSOR 1750 1450 RECOVERY RECOVERY (3)SERVICE GPM (1) CFM MODEL RPM RPM RPM 100°F 80°F 100°F 80°F VAPOR LIQUID

45 8 291 390 A 3.4 B 4.0 5 3 3 3 1 1-1/250 9 291 435 A 3.8 B 4.6 5 5 3 3 1 1-1/256 10 291 490 B 4.4 B 5.2 5 5 5 3 1 2

UNLOADING 62 11 291 535 B 4.8 B 5.8 7-1/2 5 5 5 1 2SINGLE TANK 67 12 291 580 B 5.2 B 6.2 7-1/2 5 5 5 1 2

CAR OR 72 13 291 625 B 5.6 B 6.6 7-1/2 5 5 5 1-1/4 2TRANSPORT 80 14 291 695 B 6.2 B 7.4 7-1/2 7-1/2 7-1/2 5 1-1/4 2

85 15 291 735 B 6.6 B 8.0 10 7-1/2 7-1/2 7-1/2 1-1/4 2-1/285 15 491 345 A 3.0 A 3.6 7-1/2 7-1/2 5 5 1-1/4 2-1/290 16 291 780 B 7.0 B 8.6 10 7-1/2 7-1/2 7-1/2 1-1/4 2-1/290 16 491 370 A 3.2 A 3.8 10 7-1/2 5 5 1-1/4 2-1/296 17 491 390 A 3.4 B 4.0 10 7-1/2 5 5 1-1/4 3102 18 491 415 A 3.6 B 4.4 10 7-1/2 7-1/2 7-1/2 1-1/4 3107 19 491 435 A 3.8 B 4.6 10 7-1/2 7-1/2 7-1/2 1-1/4 3110 20 491 445 B 4.0 B 4.8 10 7-1/2 7-1/2 7-1/2 1-1/4 3115 21 491 470 B 4.2 B 5.0 10 7-1/2 7-1/2 7-1/2 1-1/4 3

UNLOADING 120 22 491 490 B 4.4 B 5.2 15 10 7-1/2 7-1/2 1-1/4 3TWO OR 126 23 491 515 B 4.6 B 5.6 15 10 7-1/2 7-1/2 1-1/4 3

MORE TANK 131 24 491 535 B 4.8 B 5.8 15 10 10 7-1/2 1-1/4 3CARS AT 138 25 491 560 B 5.0 B 6.0 15 10 10 7-1/2 1-1/4 3

ONE TIME, 142 26 491 580 B 5.2 B 6.2 15 10 10 7-1/2 1-1/4 3OR LARGE 148 27 491 605 B 5.4 B 6.4 15 10 10 10 1-1/4 3

TRANSPORT 153 28 491 625 B 5.6 B 6.6 15 10 10 10 1-1/2 3WITH EXCESS 160 29 491 650 B 5.8 B 7.0 15 15 10 10 1-1/2 3FLOW VALVES 165 30 491 670 B 6.0 15 15 15 10 1-1/2 3OF ADEQUATE 165 30 691 400 B 4.4 B 5.2 15 15 10 10 1-1/2 3

CAPACITY 170 31 491 695 B 6.2 B 7.4 15 15 15 10 1-1/2 3173 31 691 420 B 4.6 B 5.6 15 15 10 10 1-1/2 3181 32 491 740 B 6.6 B 8.0 15 15 15 15 1-1/2 3180 32 691 440 B 4.8 B 5.8 15 15 10 10 1-1/2 3188 34 691 455 B 5.0 B 6.0 20 15 10 10 1-1/2 3195 35 691 475 B 5.2 B 6.2 20 15 10 10 1-1/2 3203 36 691 495 B 5.4 B 6.4 20 15 15 10 1-1/2 3211 38 691 510 B 5.6 B 6.8 20 15 15 10 1-1/2 4218 39 691 530 B 5.8 B 7.0 20 15 15 15 1-1/2 4226 41 691 550 B 6.0 A 7.0 20 15 15 15 1-1/2 4233 42 691 565 B 6.2 B 7.4 20 15 15 15 2 4

UNLOADING 240 43 691 585 B 6.4 A 7.4 20 20 15 15 2 4LARGE 248 45 691 605 B 6.6 B 8.0 20 20 15 15 2 4

TANK CAR, 255 45 691 620 B 6.8 25 20 15 15 2 4MULTIPLE 263 47 691 640 B 7.0 A 8.2 25 20 15 15 2 4VESSELS, 278 48 691 675 B 7.4 B 8.6 25 20 15 15 2 4

BARGES OR 301 54 691 730 B 8.0 B 9.4 25 20 20 15 2 4TERMINALS 323 58 691 785 B 8.6 30 25 20 20 2 4

338 60 691 820 TB9.0 A 10.6 30 25 20 20 2 4459 82 D891 580 5V 7.1 5V 8.5 40 30 30 30 3 6630 113 D891 800 5V 9.75 5V 11.8 40 40 30 3 6

AMMONIA COMPRESSOR SELECTION TABLE


20


MOVING LIQUID WITH VAPOR

The most flexible method for moving liquid ammonia is with acompressor, a device designed to handle vapor and only vapor. Howis this done? You will remember from the first chapter that creatinga different pressure between two points may move any fluid, vaporor gas. A compressor may be used to create a pressure differencebetween the vapor spaces of two tanks. If the liquid spaces of the twotanks are connected, the pressure difference exerted by vapor willcause the liquid to begin flowing from the higher pressure tank to thelower pressure tank. Figure 2, page 18.

You will also remember that changes in internal pressure of anammonia tank will result in condensation and boiling.Condensation and boiling will tend to negate the pressuredifference created by the compressor. Liquid transfer using acompressor works because vapor may be moved more quicklythan it boils off and condenses. The flow rate induced will equalthe volume of gas discharged from the compressor if a largeenough compressor is chosen to make the effect of boiling andcondensation negligible. The pressure increase through thecompressor will equal the pressure decrease due to friction in theliquid piping. Years of experience have shown that pipingdesigned to create a pressure drop of 30 psi or less works best.Higher pressure drops result in more condensation and boilingand reduced flow rates due to reduced discharge volume.

Compressors may also be used to evacuate tanks. High pressureammonia vapor in a large tank has substantial economic value thatmakes it worth recovering. Tanks that must be unloaded through adip tube (such as most railroad tank cars) leave a small liquid puddlein the tank when liquid transfer is complete. A compressor can beused to reduce the pressure in the tank to boil the puddle intorecoverable vapor. The vapor recondenses when it is fed into theliquid section of another ammonia tank (see Figure 3, Page 21).

Corken oil-free gas transfer compressors are the standard of theindustry. Models FD291 / 491 are popular for truck unloading andunloading small railroad cars. The model FD691 is suitable forunloading large railroad tank cars.

LIQUID TRANSFER AND VAPOR RECOVERY

Compressor size and speed selection is a highly inexact processwith complex interactions of a number of different variables suchas ambient temperature, pressure drops in liquid line and vaporsuction line, solar radiation, precipitation, size of the tanks and thesurface area of the tank and piping. With this many variables, the

exact performance of the compressor cannot be preciselycalculated. Corken's Compressor Selection Table, on page 19, isa fast and easy method to make an approximate selection forammonia compressors. The chart shows flows for different Corkencompressors run at different speeds with a maximum tanktemperature of 100°F and 80°F with a 30 psi pressure drop in thepiping. In only the most extreme temperature conditions will tanktemperatures exceed 100°F. A large tank heats up and cools downmuch more slowly than the surrounding atmosphere. Althoughtemperatures may frequently exceed 100°F on hot summerafternoons, tank temperatures will seldom rise this high.Therefore, the horsepower values shown in the charts are veryconservative and may be lowered for milder climates. Your localCorken distributor is usually the best source of information forideal motor sizes for the climate in your region. Corken suppliesa computer analysis showing the capacity and horsepower requiredfor different tank temperatures.

If it is important that unloading operations must be complete in a certainamount of time, a more complex analysis is required. When such ananalysis is required, contact Corken so a factory application engineermay thoroughly review the application. By inputting the tank size,pressure drops, model number, speed and gas into a special computerprogram, Corken's application engineers can determine how themachine will perform over a wide temperature range with reasonableaccuracy. Such an analysis is shown in Figures 4 and 5, pages 23 and24. This analysis is divided into three parts that clearly demonstrate howtemperature affects flow rates and vapor recovery time.

The highest liquid flow rates are achieved on hot days. This isbecause the pressure drop in the piping remains relatively constantas the temperature changes while the vapor pressure swings overa wide pressure range. The vapor pressure of ammonia is 30 psiaat 0°F and 247 psia at 110°F. The discharge pressure, P2, is theproduct vapor pressure plus the system differential pressure. InFigure 4, page 23, the 30 psi pressure drop is added to the vaporpressure (VP) to yield the discharge pressure shown in column P2.You will notice that the compression ratio (the absolute inlet vaporpressure divided by the absolute discharge pressure) rises as thetemperature falls. As the compression ratio rises with fallingtemperature, the gas passing through the compressor is squeezedinto a smaller and smaller discharge volume. As the volume at thedischarge of the compressor is reduced, the amount of liquiddisplaced by the vapor is also reduced.

21

Vapor Lines

Liquid Lines

Inlet tocompressor

Discharge fromcompressor

Inlet fromstorage tank

Four-Way Valve Operation

Discharge totank car

Compressor reducespressure in storage tank

by removing vapor

Compressor increasespressure in tank car

by adding vapor

Pressure difference betweentanks causes liquid to flow out ofthe tank car into the storage tank

Vapor Lines

Liquid line valve is closedduring vapor recovery

Inlet tocompressor

Discharge fromcompressor

Discharge tostorage tank

Four-Way Valve Operation

Inlet fromtank car

Vapor is bubbled throughliquid to help cool and

recondense itLiquid Heel

Removing vapor from tankcauses liquid heel to boil into vapor

FIGURE 2 LIQUID TRANSFER

FIGURE 3 VAPOR RECOVERY



22



When the liquid in a tank is unloaded through a dip tube, liquidtransfer will cease when the liquid level falls beneath the bottom ofthis tube. The residual puddle is called a "liquid heel". By reversingthe direction of vapor flow and blocking the liquid line as shown inFigure 3, page 18, this liquid may be recovered. By withdrawingvapor out of the tank, the liquid will begin to boil into vapor toreplace the vapor being removed. This process is called "boil-out".Boil-out is completed most rapidly on hot days. The high vaporpressure on hot days gives the gas a higher density than on cold days.It takes a larger quantity of liquid to replace a cubic foot of highdensity vapor than low density vapor.

When boil-out is completed a substantial amount of gas is left in thetank in a vapor state. This vapor is equivalent to a substantial amountof liquid of significant economic value. As a rule of thumb in theindustry, tank cars should be evacuated to 40 psia. Alternately, a finalevacuation pressure of 25 to 30 percent of original tank car pressureis a good value for most any liquid gas. Evacuation pressures lowerthan this will not pay for the energy required to run the compressorand generally should not be considered unless factors other thaneconomics are being considered. The vapor recovery procedurerequires the most time on hot days because of the high initial vaporpressure in the tank. The recovered vapor should be bubbled upthrough the liquid section of the receiver tank to recondense thevapor to liquid. The maximum horsepower requirement for thecompressor occurs when the tank has been evacuated toapproximately 50 percent of full vapor pressure. Larger motors arerequired to do vapor recovery in hot climates.

23

LIQUID TRANSFER PHASET1 VP P2 T2 CR VE Z Z ACFM ACFM Lb/Hr GPM BHP Time°F psia psia °F % In Out In Out Liquid Min.0 30 60 82 2.0 88 .97 .97 27.0 13.5 31,317 101 5.7 27610 39 69 78 1.8 90 .96 .96 27.4 15.5 35,930 116 6.2 24120 48 78 78 1.6 91 .96 .95 27.6 17.0 39,481 127 6.6 21930 60 90 79 1.5 91 .95 .95 27.9 18.6 43,111 139 7.0 20140 73 103 82 1.4 92 .94 .94 28.0 19.9 46,087 149 7.4 18850 89 119 86 1.3 92 .94 .93 28.1 21.1 48,852 157 7.9 17760 108 138 91 1.3 92 .93 .92 28.2 22.1 51,296 165 8.4 16970 129 159 97 1.2 93 .92 .91 28.3 23.0 53,312 172 8.9 16280 153 183 103 1.2 93 .91 .90 28.4 23.7 55,042 177 9.5 15790 181 211 110 1.2 93 .90 .89 28.4 24.4 56,554 182 10.1 153100 212 242 118 1.1 93 .88 .88 28.4 24.9 57,813 186 10.8 150110 247 277 126 1.1 93 .87 .87 28.5 25.4 58,888 190 11.5 147

BOIL-OFF PHASEEquiv. LiquidVapor Rec.

T1 VP P2 T2 CR VE Z Z ACFM Vol Rate BHP Time°F psia psia °F % In Out In Ft3 GPM Min.0 30 38 26 1.3 93 .97 .97 28.5 7,994 1 3.8 28110 39 47 31 1.2 94 .96 .96 28.6 6,242 1 4.1 21820 48 56 38 1.2 94 .96 .96 28.6 5,150 1 4.3 18030 60 68 45 1.1 94 .95 .95 28.7 4,174 1 4.7 14640 73 81 52 1.1 94 .94 .94 28.7 3,475 1 5.0 12150 89 97 60 1.1 94 .94 .93 28.7 2,882 2 5.4 10060 108 116 69 1.1 94 .93 .93 28.7 2,397 2 5.8 8370 129 137 78 1.1 94 .92 .92 28.7 2,024 2 6.2 7080 153 161 87 1.1 94 .91 .91 28.7 1,719 3 6.8 6090 181 189 96 1.0 94 .90 .89 28.7 1,461 3 7.3 51100 212 220 105 1.0 94 .88 .88 28.7 1,253 4 8.0 44110 247 255 114 1.0 94 .87 .87 28.7 1,079 4 8.6 38

VAPOR RECOVERY PROCESSP1

P1 at Equiv. Liquid (gal) TotalT1 VP P2 T2 VE% VE% ACFM ACFM Z in Z in VE Max

Actual Recovered ClaimableBHP Time Time

°F psia psia °F Initial Final Initial Final Initial Final VE=0 VHP Max Min. Hrs.10 39 47 31 94 94 28.6 28.6 .96 .96 2 39 116.6 22.7 109.7 4.1 33 8.220 48 56 64 94 92 28.6 28.1 .96 .97 3 39 141.4 49.1 133.3 5.1 46 7.430 60 68 97 94 90 28.7 27.5 .95 .97 3 40 174.4 81.7 164.7 6.1 79 7.140 73 81 132 94 88 28.7 26.8 .94 .97 4 40 209.5 118.3 198.3 7.1 110 7.050 89 97 169 94 85 28.7 26.1 .94 .97 5 40 252.6 162.0 239.4 8.1 142 7.060 108 116 207 94 83 28.7 25.2 .93 .97 6 49 303.7 213.3 288.2 9.3 174 7.170 129 137 247 94 80 28.7 24.3 .92 .98 7 59 359.6 270.1 341.6 10.5 206 7.380 153 161 287 94 76 28.7 23.3 .91 .98 8 70 423.4 334.5 402.6 12.0 238 7.690 181 189 358 94 68 28.7 20.9 .90 .98 10 83 498.2 421.7 474.3 13.7 272 7.9100 212 220 399 94 64 28.7 19.6 .88 .98 11 99 580.9 503.5 553.6 15.6 307 8.3110 247 255 440 94 60 28.7 18.3 .87 .98 13 116 674.9 596.0 643.6 17.7 344 8.8

Assumptions of Calculations:1. Pressure drops remain constant.2. Induced flow based on isothermal compression. 3. BHP and temperature are based on adiabatic compression.4. Compressibility effects are considred in calculations. 5. Heat transfer is sufficient to maintain constant tank temperature during boil-out.

RPM: 700

PD: 30.5

MAWP: 335 psia

Tank Volume: 33,000 Gallonsand is 85 percent full

Gas: Anhydrous Ammonia(NH3)

n: 1.31

Molecular weight: 17.03

Critical pressure: 1,636 psia

Critical temperature: 730° R

30 psi drop in liquid transfer system

Total liquid volumetransferred = 27,885 gallons(84.5 of total tank volume)

Liquid heel: 165 gallons(0.5 percent of total tankvolume)

35 psia desired evacuation pressure

8 psi drop in vapor recovery system

FIGURE 4 – LIQUEFIED GAS TRANSFER COMPRESSOR WORKSHEET – MODEL 491


24

FIGURE 5 – LIQUEFIED GAS TRANSFER COMPRESSOR WORKSHEET – MODEL 691


LIQUID TRANSFER PHASET1 VP P2 T2 CR VE Z Z ACFM ACFM Lb/Hr GPM BHP Time°F psia psia °F % In Out In Out Liquid Min.0 30 60 82 2.0 86 .97 .97 48.9 24.5 56,781 183 10.4 15210 39 69 78 1.8 88 .96 .96 50.0 28.3 65,594 211 11.1 13220 48 78 78 1.6 89 .96 .95 50.7 31.2 72,388 233 11.7 12030 60 90 79 1.5 90 .95 .95 51.3 34.2 79,337 256 12.3 10940 73 103 82 1.4 91 .94 .94 51.7 36.6 85,038 274 12.9 10250 89 119 86 1.3 91 .94 .93 52.0 38.9 90,338 291 13.5 9660 108 138 91 1.3 92 .93 .92 52.3 40.9 95,026 306 14.2 9170 129 159 97 1.2 92 .92 .91 52.5 42.6 98,893 319 14.8 8780 153 183 103 1.2 92 .91 .90 52.7 44.0 102,213 329 15.6 8590 181 211 110 1.2 93 .90 .89 52.8 45.3 105,117 339 16.4 82100 212 242 118 1.1 93 .88 .88 52.9 46.3 107,535 347 17.2 80110 247 277 126 1.1 93 .87 .87 53.0 47.2 109,600 353 18.1 79

BOIL-OFF PHASEEquiv. LiquidVapor Rec.

T1 VP P2 T2 CR VE Z Z ACFM Vol Rate BHP Time°F psia psia °F % In Out In Ft3 GPM Min.0 30 38 26 1.3 93 .97 .97 52.8 7,994 1 7.0 15110 39 47 31 1.2 93 .96 .96 53.1 6,242 1 7.3 11820 48 56 38 1.2 93 .96 .96 53.2 5,150 2 7.6 9730 60 68 45 1.1 94 .95 .95 53.4 4,174 2 8.0 7840 73 81 52 1.1 94 .94 .94 53.4 3,475 3 8.4 6550 89 97 60 1.1 94 .94 .93 53.5 2,882 3 8.8 5460 108 116 69 1.1 94 .93 .93 53.5 2,397 4 9.3 4570 129 137 78 1.1 94 .92 .92 53.6 2,024 4 9.9 3880 153 161 87 1.1 94 .91 .91 53.6 1,719 5 10.5 3290 181 189 96 1.0 94 .90 .89 53.6 1,461 6 11.2 27100 212 220 105 1.0 94 .88 .88 53.6 1,253 7 12.0 23110 247 255 114 1.0 94 .87 .87 53.5 1,079 8 12.8 20

VAPOR RECOVERY PROCESSP1

P1 at Equiv. Liquid (gal) TotalT1 VP P2 T2 VE% VE% ACFM ACFM Z in Z in VE Max

Actual Recovered ClaimableBHP Time Time

°F psia psia °F Initial Final Initial Final Initial Final VE=0 VHP Max Min. Hrs.10 39 47 31 93 93 53.1 53.1 .96 .96 3 39 116.6 21.0 106.9 7.3 16 4.420 48 56 62 93 91 53.2 51.9 .96 .97 4 39 141.4 45.8 130.0 9.0 25 4.030 60 68 93 94 89 53.4 50.6 .95 .97 5 41 174.4 76.7 160.9 10.8 43 3.840 73 81 125 94 86 53.4 49.1 .94 .97 6 42 209.5 111.7 193.8 12.6 60 3.850 89 97 184 94 80 53.5 45.5 .94 .97 7 43 252.6 168.8 234.2 14.4 78 3.860 108 116 219 94 76 53.5 43.5 .93 .98 8 52 303.7 217.9 282.0 16.4 97 3.970 129 137 255 94 72 53.6 41.3 .92 .98 10 63 359.6 272.2 334.4 18.5 115 4.080 153 161 291 94 68 53.6 39.1 .91 .98 11 75 423.4 334.1 394.5 21.0 134 4.290 181 189 352 94 60 53.6 34.1 .90 .98 13 75 498.2 416.9 464.7 23.9 155 4.4100 212 220 387 94 55 53.6 31.6 .88 .98 16 89 580.9 496.3 542.2 27.1 177 4.7110 247 255 443 94 47 53.5 26.5 .87 .98 19 105 674.9 594.4 630.4 30.7 202 5.0

Assumptions of Calculations:1. Pressure drops remain constant.2. Induced flow based on isothermal compression. 3. BHP and temperature are based on adiabatic compression.4. Compressibility effects are considred in calculations. 5. Heat transfer is sufficient to maintain constant tank temperature during boil-out.

RPM: 775

PD: 57.1

MAWP: 335 psia

Tank Volume: 33,000 Gallonsand is 85 percent full

Gas: Anhydrous Ammonia(NH3)

n: 1.31

Molecular weight: 17.03

Critical pressure: 1,636 psia

Critical temperature: 730° R

30 psi drop in liquid transfer system

Total liquid volumetransferred = 27,885 gallons(84.5 of total tank volume)

Liquid heel: 165 gallons(0.5 percent of total tankvolume)

35 psia desired evacuation pressure

8 psi drop in vapor recovery system

25

Corken vertical compressors are similar in many ways to the smallvertical lubricated compressors that have been used for years.However, Corken oil-free compressors are, by design, much tallerthan most other compressor types. This also means that the verticalcenter of gravity is considerably higher. These factors amplify themagnitude of any vibration present, and must be considered whenselecting a mounting location for your compressor.

Corken recommends securing the compressor on a concrete pad orsturdy structural steel mounting base.

Most Corken units do fine with the baseplate mounted directly to asolid reinforced concrete slab. Special attention should be given tothe large vertical compressors (models 591, 691, 791, and 891).These units require very firm foundations due to their vertical height.The HG600 series is a horizontal balanced-opposed unit, but wesuggest that the same foundation guidelines be followed.

Generally speaking, the larger the foundation, the less likely you areto have vibration or shaking problems.

Permanent anchor bolts or “J” bolts embedded in the foundation willusually provide excellent stability. Grouting the baseplate into yourfoundation and checking the mounting bolts for tightness at frequentintervals is highly recommended.

As a rule of thumb, when preparing the foundation, the mounting slabshould be a minimum of eight inches thick, with the overall lengthand width four inches longer and wider on each side of the baseplate.

The following illustrations show some basic guidelines to follow.The mounting variations shown are guidelines only. A properlyengineered foundation should be installed before putting your newcompressors into service. A special baseplate is required on some ofthe illustrations.

IMPORTANT: Any proposed isolation mounting arrangement mustbe properly engineered. Failure to do so will most likely increase theseverity of the problem.

The compressor must not support any significant piping weight, sothe piping must be properly supported. The use of flexibleconnections at the compressor is highly recommended. Rigid,unsupported piping combined with a poor foundation will result insevere vibration problems.

Corken baseplates come with anchor-bolt mounting holes. Use allmounting holes when installing baseplates.

If you have any questions about the compressor foundation for yourinstallation, please feel free to contact Corken.

COMPRESSOR FOUNDATION DESIGN


26



Do not suspend baseplate with spacers or shims allowingsupport only at the anchor bolts.

3. NO 4. YES

5. NO 6. YES

Support entire length of base to slab. Some shims may berequired on an unlevel slab.

Lead anchors will not holdpermanently.

If anchors must be used, theyshould be the type with a steelstud and sleeve.

Permanent anchor bolts imbedded in the concrete slab is a verygood installation method. Grouting the baseplate to the slab ishighly recommended.

Anchors or lags with a shallow mounting will pull loose.Be sure the existing floor is solid (special considerationshould be given to units on suspended floors).

If the existing floor is too weak to support compressor mounting,cut out the existing floor and mount a separate foundationdirectly on the ground.

1. NO 2. YES

27

7. NO 8. YES

Rubber mounts or pads are generally not recommended. NOTE: A special rigid baseplate is required on this mounting.Installing mounts at the compressor’s center of gravityis effective on smaller units (models 91 - 491).

9. NO 10. NO

11. YES 12. YES

If skid mounting, do not mount the compressor assembly onshallow beams or angle iron.

Do not mount the compressor assembly across beams withoutcenter support.

Mount the baseplate so that the beam or channel providessupport along the entire length of the baseplate. NOTE: Crossbeams should be full depth of main beams. Thebaseplate is normally welded to the skid directly over thevertical web of the support beam.

The compressor must not support any significant piping weight,so the piping must be properly supported. The use of flexibleconnections at the compressor is highly recommended. Rigid,unsupported piping combined with a poor foundation will resultin severe vibration problems.



28

29

* Above differential pressures are based on a .65 specific gravity.** Consult FactoryNeoprene®, Viton®, Kalrez® and Teflon® are registered trademarks of the DuPont Company.

SPECIFICATIONS MODEL

10 20 30 40 50 60Number of Stages 1 to 8

Inlet Flange 1-1/2 (40) 2-1/2 (65) 2-1/2 (65) 3 (80) 4 (100) 4 (100)inches (mm)

Outlet Flangeinches (mm) 3/4 (20) 1-1/4 (32) 1-1/4 (32) 1-1/2 (40) 2 (50) 2-1/2 (65)

RPM-60 hz 1150/1750 1150/1750 1150/1750 1150/1750 1150/1750 1150/1750

RPM-50 hz 1450 1450 1450 1450 1450 1450

Maximum WorkingPressure psig (bar) 580 (40) 580 (40) 580 (40) 580 (40) 580 (40) 580 (40)

Differential Pressure* 7 (.5) 7 (.5) 4 (.3) 7 (.5) 7 (.5) 7 (.5)Range psi (bar) 200 (14) 325 (21) 240 (16) 230 (16) 230 (16) 230 (16)

Min. Temp. °F (°C) -40° (-40°) -40° (-40°) -40° (-40°) -40° (-40°) -40° (-40°) -40° (-40°)

Max. Temp. °F (°C) 428° (220°) 428° (220°) 428° (220°) 428° (220°) 428° (220°) 428° (220°)

NPSH Range ft (m) 1.0 (.3) 1.3 (.4) 1.0 (.3) 1.0 (.3) 1.0 (.3) 1.0 (.3)

13 (4) 3.3 (1) 6.6 (2) 8.2 (2.5) 8.2 (2.5) 8.2 (2.5)

Maximum Viscosityssu (cst) 1050 (230) 1050 (230) 1050 (230) 1050 (230) 1050 (230) 1050 (230)

Maximum Proportionof Gas Allowable 50% 50% 50% 50% 50% 50%

ANSI Flange Option ** Yes Yes Yes Yes Yes

DIN Flange Option Yes Yes Yes Yes Yes Yes

Casing Material Options Ductile Iron, Cast Iron, Stainless Steel

Impeller Material Options Bronze, Steel, Stainless Steel

O-Ring Material Options Neoprene®, Viton®, Teflon®, Ethylene-Propylene, Kalrez®

Double Seal Option Yes Yes Yes Yes Yes Yes

Magnetic Drive Option Yes Yes Yes Yes Yes No

High Temp. Option Yes Yes Yes Yes Yes Yes

Internal Relief Option No No No No No No

Corken’s side channel (sc-series) product line is the optimal offering forammonia transfer. This continuous duty pump, which operates at lowerspeeds than most impeller designs, will allow for a high percentage ofentrained vapor (up to 50 percent) and is extremely forgiving when inletconditions are questionable (NPSHr as low as 1 ft.).

In addition to being suitable for continuous duty operation, thispump is also capable of differential pressures up to 325 psi foranhydrous ammonia. While many pump designs will not offer asealless option for liquefied gas applications, our side channelmagnetic drive (scm) pump is not only suitable for liquefied gastransfer, it will also operate under the same extreme inlet conditionsas the sealed model.

SC-SERIES SIDE CHANNEL PUMPS

Guide to Pump Selection 2

30

The design of the side-channel pump allows for the transfer ofliquid-gas mixtures with up to 50 percent vapor; thereforeeliminating possible air or vapor locking that can occur in otherpump designs. A special suction impeller lowers the NPSHrequirement for the pump.

The side-channel pump design is similar to a regenerative turbinein that the impeller makes regenerative passes through the liquid.However, the actual design of the impeller and casing as well as theprinciples of operation differ greatly. The side-channel pump has achannel only in the discharge stage casing (A) and a flat surfacewhich is flush with the impeller on the suction stage casing (B). Astar-shaped impeller (C) is keyed to the shaft and is axially balancedthrough equalization holes (D) in the hub of the impeller.

The liquid or liquid/vapor mixture enters each stage of the pumpthrough the inlet port (E). Once the pump is initially filled withliquid, the pump will provide a siphoning effect at the inlet port. Theeffect is similar to what happens in water ring pumps. The waterremaining in the pump casing forms a type of water ring with a freesurface. A venturi effect is created by the rotation of the impeller andthe free surface of the water, thus pulling the liquid into the casing.

After the liquid is pulled through the inlet port, it is forced to theouter periphery of the impeller blade by centrifugal action. It isthrough this centrifugal action that the liquid is accelerated andforced into the side channel. The liquid then flows along thesemicircular contour of the side channel from the outermost pointto the innermost point until once again it is accelerated by theimpeller blade. The liquid moves several times between the impellerand the side channel. Thus the rotating impeller makes several

regenerative passes until the liquid reaches the outlet port. Thespeed of the impeller along with the centrifugal action impartenergy to the liquid through the exchange of momentum, thusallowing the pump to build pressure.

The side channel leads directly to the outlet port (F). At the outletport, the main channel ends and a smaller minichannel (G) begins.At the point where the mini-channel ends, there is a small secondarydischarge port (H) level with the base of the impeller blades.

As the liquid is forced to the periphery through centrifugal action dueto its density, the vapor within the liquid stream tends to remain at thebase of the impeller blades since it has a much lower density. The mainportion of liquid and possibly some vapor, depending on the mix, isdischarged through the outlet port. A small portion of the liquid flowfollows the mini-channel and eventually is forced into the areabetween the impeller blades. The remaining vapor which was notdrawn through the outlet port resides at the base of the impellerblades. At the end of the mini-channel, as the liquid is forced into thearea between the blades, the area between and around the impellerblade is reduced. The liquid between the blades displaces and thuscompresses the remaining vapor at the base of the impeller blades.The compressed vapor is then forced through the secondary dischargeport where it combines with the liquid discharged through the outletport as it is pulled into the next stage or discharged from the pump.Thus entrained vapor is moved through each stage of the pump.

Each subsequent stage operates under the same principle. Thenumber of stages can be varied to meet the required discharge head.When multiple stages are required, the relative positions of the stageoutlet ports are radially staggered to balance shaft loads.

Item Description

A Discharge Stage CasingB Suction Stage CasingC ImpellerD Equalization HolesE Inlet PortF Outlet PortG Mini-ChannelH Secondary Discharge Port

Liquid-VaporMixture

A

F GH C D

E

B

Vapor Liquid

PRINCIPLE OF SIDE CHANNEL OPERATION

Guide to Pump Selection2

31

SC/SCM OVERVIEW GRAPH–1750 RPM


30 4050 60H

ead

Fee

t

GPM (L /min)

10(38)

20(76)

30(114)

40(151)

50(189)

60(227)

70(265)

80(303)

90(341)

110(416)

120(454)

130(492)

140(530)

150(568)

160(606)

170(644)

100(379)

180(681)

190(719)

0(0)

600

1200

1100

1000

900

800

700

500

400

300

200

100

0

183

366

335

305

274

244

213

152

122

91

61

300

Head Meters

10

20

1040

50 60

NP

SH

R F

eet

GPM (L /min)

10(38)

20(76)

30(114)

40(151)

50(189)

60(227)

70(265)

80(303)

90(341)

110(416)

120(454)

130(492)

140(530)

150(568)

160(606)

170(644)

100(379)

180(681)

190(719)

0(0)

14

12

10

8

6

4

2

0

4.3

3.7

3.0

2.4

1.8

1.2

0.6

0

NPSHR Meters

2030

Po

wer

Req

uir

ed (h

p)

GPM (L /min)

30

20

10

0

22.4

14.9

7.5

0

0(0)

10(38)

20(76)

30(114)

40(151)

50(189)

40

(kW)

3020

10

25

15

5

18.6

11.2

3.7

60(227 )

70(265)

Po

wer

Req

uir

ed (h

p)

GPM (L /min)

10090807060504030

20100

74.667.159.7

37.3

52.244.7

3022.414.9

7.5

0

70(265)

90(341)

100(379)

110(416)

120(454)

130(492)

140(530)

150(568)

160(606)

170(644)

180(681)

60

50

(kW)

110120

80(303)

190(719)

82.089.5

32

SC/SCM OVERVIEW GRAPH–1150 RPM


30 4050 60H

ead

Fee

t

GPM (L /min)

10(38)

20(76)

30(114)

40(151)

50(189)

60(227)

70(265)

80(303)

90(341)

110(416)

120(454)

130(492)

140(530)

150(568)

160(606)

170(644)

100(379)

180(681)

190(719)

0(0)

600

1200

1100

1000

900

800

700

500

400

300

200

100

0

183

366

335

305

274

244

213

152

122

91

61

300

Head Meters

10

20

1040

50 60

NP

SH

R F

eet

GPM (L /min)

10(38)

20(76)

30(114)

40(151)

50(189)

60(227)

70(265)

80(303)

90(341)

110(416)

120(454)

130(492)

140(530)

150(568)

160(606)

170(644)

100(379)

180(681)

190(719)

0(0)

14

12

10

8

6

4

2

0

4.3

3.7

3.0

2.4

1.8

1.2

0.6

0

NPSHR Meters

2030

Po

wer

Req

uir

ed (h

p)

GPM (L /min)

30

20

10

0

22.4

14.9

7.5

0

0(0)

10(38)

20(76)

30(114)

40(151)

50(189)

40

(kW)

3020

10

25

15

5

18.6

11.2

3.7

60(227 )

70(265)

Po

wer

Req

uir

ed (h

p)

GPM (L /min)

10090807060504030

20100

74.667.159.7

37.3

52.244.7

3022.414.9

7.5

0

70(265)

90(341)

100(379)

110(416)

120(454)

130(492)

140(530)

150(568)

160(606)

170(644)

180(681)

60

50

(kW)

110120

80(303)

190(719)

82.089.5

33

INSTRUCTIONS FOR SELECTION OF MECHANICAL SEAL MODEL


1. Turn to the performance curve page that corresponds with the pump series and speed that you noted from the overview on pages 31 & 32.

Series 1750 RPM 1150 RPM10 page 36 page 3720 page 38 page 3930 page 40 page 4140 page 42 page 4350 page 44 page 4560 page 46 page 47

2. Locate the differential head value ( ) on the left side of Graph 1.

NOTE: Differential pressure = pump discharge pressure – pump inlet pressure.

3. From that point, move horizontally to the right until you intersect one of the eight diagonal lines. Move down vertically from the pointof intersection to the bottom of the graph to determine if the flow rate at that point comes close to the desired flow rate. If it does not,continue horizontally from the current point of intersection until you reach the next diagonal line. Repeat until you determine whichline most closely matches the desired flow at the required differential head. Make note of the number that corresponds with that particularline. This is the specific model that most closely meets your application.

4. From the point of intersection on Graph 1, move vertically down to Graph 2. Continue to move down until you intersect the diagonalline that corresponds with the specific model that you selected above.

5. From this point of intersection, move horizontally to the left side of the graph and note the horsepower value. Take this value and multiplyit by the specific gravity of the liquid to be pumped. The value that you calculate is the brake horsepower required to operate this pumpin the given application. You must select a motor with a horsepower greater than (or at a minimum equal to) this value.

6. Now proceed straight vertically down to Graph 3, the point on the NPSH line that corresponds with the flow rate that you determinedthe specific model would provide. Move horizontally to the left and note the value of NPSH required. This value must be less than thenpsh available. If it is not, repeat procedures to try to locate a different model, or contact your distributor or Corken for assistance.

head feet = 2.31 x psi (differential)

specific gravity of liquid pumped

34

INSTRUCTIONS FOR SELECTION OF MAGNETIC DRIVE MODEL


1. Turn to the performance curve page that corresponds with the pump series and speed that you noted from the overview on pages 31 & 32.

Series 1750 RPM 1150 RPM10 page 36 page 3720 page 38 page 3930 page 40 page 4140 page 42 page 4350 page 44 page 4560 page 46 page 47

2. Locate the differential head value on the left side of Graph 1.

3. From that point, move horizontally to the right until you intersect one of the eight diagonal lines. Move down vertically from the pointof intersection to the bottom of the graph to determine if the flow rate at that point comes close to the desired flow rate. If it does not,continue horizontally from the current point of intersection until you reach the next diagonal line. Repeat until you determine whichline most closely matches the desired flow at the required differential head. Make note of the number that corresponds with that particularline. This is the specific model that most closely meets your application.

4. From the point of intersection on Graph 1, move vertically down to Graph 2. Continue to move down until you intersect the diagonalline that corresponds with the specific model that you selected above.

5. From this point of intersection, move horizontally to the left side of the graph and note the horsepower value.

6. Multiply this value by the specific gravity of the liquid to be pumped to calculate the power demand of the pump.

7. Refer to the magnetic coupling selection table on page 34.

8. Find the row in table 1 listed as MAXIMUM POWER DEMAND OF PUMP. Proceed to the right until you locate a hp value greaterthan the power demand that you calculated in step 6.

9. Look at table 2 in the same column to see if there is a dot in the same row as the pump series that you have selected. If so, proceed to step10. If not, repeat step 8 (continue to the right). Note: There are occasions when there is not a magnetic coupling with enough torque to handlea specific application. For this case, consider whether a sealed unit is acceptable or consult your distributor or the factory for advice.

10. Look at table 3 in the same column. Locate the maximum working pressure of the separation canister for the magnetic coupling at thetemperature value that exceeds your operating temperature. This pressure value must be greater than the discharge pressure of yourapplication. Note that the hastelloy canister at the bottom of table 3 offers higher pressure capabilities. When the discharge pressure ofyour application exceeds the maximum of the standard stainless canister.

11. Once you have located a magnetic coupling size that meets the above criteria, add the value in the POWER LOSS row (table 1) to yourvalue calculated in step 6.

12. Select a motor size greater than the value just calculated, but no larger than the value in the row that is titled MAXIMUM MOTOR SIZE.Make note of the coupling size that you have selected.

13. Return to performance curve page, proceed straight down to graph 3. Find the point on the line that corresponds with the flow rate that youdetermined the specific model will provide. Move horizontally to the left and note the value of NPSH required. This value must be less thanthe NPSH available. If it is not, repeat procedures to try to locate a different model, or contact your distributor or Corken for assistance.

35

Coupling Size 12 14 16 22 24 26 36 38

Stainless 70°F/20°C 470 470 470 305 305 305 N/A N/ACanister 210°F/100°C 430 430 430 275 275 275 N/A N/A(Standard) 300°F/150°C 400 400 400 260 260 260 N/A N/A

390°F/200°C 375 375 375 240 240 240 N/A N/AHastelloy 70°F/20°C 580 580 580 420 420 420 420 420Canister 210°F/100°C 580 580 580 390 390 390 395 395

300°F/150°C 575 575 575 370 370 370 380 380390°F/200°C 545 545 545 350 350 350 370 370

Coupling Size 12 14 16 22 24 26 36 38

Maximum Power Demand 1.1 2.6 3.8 2.6 7.6 11.3 16.8 28.5of Pump (hp)Power Loss in Magnet (hp) 0.2 0.3 0.3 0.3 0.6 0.9 1.2 1.5Maximum Motor Size 1.5 3.0 5.0 5.0 10.0 15.0 25.0 30.0

Above Couplings can be used for pump models with check marks below in the same column.

Maximum allowable working pressure (psig) for magnetic coupling at various temperatures.

Table 2Pump Series

Coupling Size 12 14 16 22 24 26 36 38

SCM10 • • •SCM20/SCM30 • • • • • •SCM40 • • • • •SCM50 • • • • •

Table 3Separation Canisters

Table 1Coupling Characteristics

MAGNETIC COUPLING SELECTION TABLE


36

0

700

6.5 13.512.511.510.59.58.57.5

600

500

400

300

200

100

Q (U.S. gpm)

GRAPH 1

GRAPH 2

GRAPH 3

H (f

t)

11

12

13

14

15

16

17

18

0

7

6.50 13.5012.5011.5010.509.508.507.50

6

5

4

3

2

1

Q (U.S. gpm)

P (h

p)N

ote:

Mul

tiply

Pow

er b

y S

peci

fic G

ravi

ty

11

12

13

14

15

16

17

18

02468

101214

6.50 7.50 8.50 9.50 10.50 11.50 12.50 13.50

Q (U.S. gpm)

NP

SH

(ft)

SC/SCM10 SERIES - 1750 RPM


37

0

100

200

300

400

1.0 2.0 3.0 4.0 5.0 6.0 7.0 8.0

18

17

16

15

14

13

12

11

Q (U.S. gpm)

H (

ft)

0.00

2.50

2.00

1.50

1.00

0.50

1.0 2.0 3.0 4.0 5.0

Q (U.S. gpm)

P (h

p)N

ote:

Mul

tiply

Pow

er b

y S

peci

fic G

ravi

ty

6.0 7.0 8.0

17

16

15

18

14

13

12

11

NP

SH

(ft)

0.0

5.0

4.0

3.0

2.0

1.0

1.0 2.0 3.0 4.0 5.0

Q (U.S. gpm)

6.0 7.0 8.0

GRAPH 1

GRAPH 2

GRAPH 3



38

0

100

200

300

400

500

600

700

800

900

1000

1100

13 14 16 18 20 22 24 2615 17 19 21 23 25 27

Q (U.S. gpm)

H (f

t)

0

2

4

6

8

10

12

14

16

18

13 14 16 18 20 22 24 2615 17 19 21 23 25 27

13 14 16 18 20 22 24 2615 17 19 21 23 25 27

Q (U.S. gpm)

P (h

p)N

ote:

Mul

tiply

Pow

er b

y S

peci

fic G

ravi

ty

012345

9.50

Q (U.S. gpm)

NP

SH

(ft)

28

27

26

25

24

23

22

21

28

27

26

25

24

23

22

21

GRAPH 1

GRAPH 2

GRAPH 3



39

0

21

22

23

24

25

26

27

28

100

200

300

400

500

600

4.0 5.0 6.0 7.0 8.0 9.0 10.0 11.0 12.0 13.0 14.0 15.0 16.0

Q (U.S. gpm)

H (f

t)

0

21

22

23

24

25

26

27

28

1

2

3

4

5

6

4.0 5.0 6.0 7.0 8.0 9.0 10.0 11.0 12.0 13.0 14.0 15.0 16.0

Q (U.S. gpm)

P (h

p)N

ote:

Mul

tiply

Pow

er b

y S

peci

fic G

ravi

ty

Q (U.S. gpm)

0

0.5

1.0

1.5

2.0

4.0 5.0 6.0 7.0 8.0 9.0 10.0 11.0 12.0 13.0 14.0 15.0 16.0

NP

SH

(ft)

GRAPH 1

GRAPH 2

GRAPH 3



40

0

100

200

300

400

500

600

700

800

900

24.5 25.5 26.5 27.5 28.5 29.5 30.5 31.5 32.5 33.5 34.5 35.5 36.5 37.5 38.5 39.5 40.5

24.5 25.5 26.5 27.5 28.5 29.5 30.5 31.5 32.5 33.5 34.5 35.5 36.5 37.5 38.5 39.5 40.5

25.524.5 26.5 27.5 28.5 29.5 30.5 31.5 32.5 33.5 34.5 35.5 36.5 37.5 38.5 39.5 40.5

Q (U.S. gpm)

H (f

t)

0

2

4

6

8

10

12

14

16

18

20

Q (U.S. gpm)

P (h

p)N

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02468

10

Q (U.S. gpm)

NP

SH

(ft)

35

34

33

32

31

38

37

36

35

34

33

32

31

36

37

38

GRAPH 1

GRAPH 2

GRAPH 3



41

0

50

100

150

200

250

300

350

400

450

31

32

33

34

35

36

37

38

13.0 14.0 15.0 16.0 17.0 18.0 20.0 21.0 22.0 23.0 24.0 25.0 26.0

Q (U.S. gpm)

H (f

t)

31

32

33

34

35

36

37

38

13.00

1

2

3

4

5

6

14.0 15.0 16.0 17.0 18.0 20.0 21.0 22.0 23.0 24.0 25.0 26.0

Q (U.S. gpm)

P (h

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13.00

1.0

2.0

3.0

4.0

14.0 15.0 16.0 17.0 18.0 20.0 21.0 22.0 23.0 24.0 25.0 26.0

Q (U.S. gpm)

NP

SH

(ft)

GRAPH 1

GRAPH 2

GRAPH 3



42

0

100

200

300

400

500

600

700

800

900

46.5 48.5 50.5 52.5 54.5 56.5 58.5 60.5 62.5 64.5 66.5

Q (U.S. gpm)

H (f

t)

02

4

6

8

10

12

14

16

1820

22

24

26

28

30

Q (U.S. gpm)

P (h

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02468

10

Q (U.S. gpm)

NP

SH

(ft)

46.5 48.5 50.5 52.5 54.5 56.5 58.5 60.5 62.5 64.5 66.5

46.5 48.5 50.5 52.5 54.5 56.5 58.5 60.5 62.5 64.5 66.5

41

42

43

44

45

46

47

48

41

42

43

44

45

46

47

48

GRAPH 1

GRAPH 2

GRAPH 3



43

0

50

10041

42

43

44

45

46

47

48

150

200

250

300

350

400

28.5 30.5 32.529.5 31.5 33.5 34.5 35.5 36.5 37.5 38.5 39.5 40.5 41.5 42.5

Q (U.S. gpm)

H (f

t)

0

1

241

42

43

44

45

46

47

48

3

4

5

6

7

8

9

28.5 30.5 32.529.5 31.5 33.5 34.5 35.5 36.5 37.5 38.5 39.5 40.5 41.5 42.5

Q (U.S. gpm)

P (h

p)N

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0.00.51.01.52.02.5

28.5 30.5 32.529.5 31.5 33.5 34.5 35.5 36.5 37.5 38.5 39.5 40.5 41.5 42.5

Q (U.S. gpm)

NP

SH

(ft)

GRAPH 1

GRAPH 2

GRAPH 3



44

0

300

200

100

400

51

52

53

54

55

56

57

58

51

52

53

54

55

56

57

58

500

600

700

800

900

1000

78 82 8680 84 88 90 92 94 96 98 100 102 104 106 108 110 112 114

Q (U.S. gpm)

H (f

t)

0

30

35

40

45

50

5

10

15

20

25

55

60

65

70

Q (U.S. gpm)

P (h

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02468

1012

Q (U.S. gpm)

NP

SH

(ft)

78 82 8680 84 88 90 92 94 96 98 100 102 104 106 108 110 112 114

78 82 8680 84 88 90 92 94 96 98 100 102 104 106 108 110 112 114

GRAPH 1

GRAPH 2

GRAPH 3



45

0

50

100

150

200

250

300

350

400

450

500

550

51

52

53

54

55

56

57

58

Q (U.S. gpm)

H (f

t)

51

52

53

54

55

56

57

58

0

6

4

2

8

10

12

14

16

22

20

18

Q (U.S. gpm)

P (h

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0

1

2

3

4

Q (U.S. gpm)

NP

SH

(ft)

46 48 50 52 54 56 58 60 62 64 66 68 70

46 48 50 52 54 56 58 60 62 64 66 68 70

46 48 50 52 54 56 58 60 62 64 66 68 70

GRAPH 1

GRAPH 2

GRAPH 3



46

0

300

200

100

400

61

62

63

64

65

66

67

68

61

62

63

64

65

66

67

68

500

600

700

800

900

1000

1100

1200

125 135 145130 140 150 155 160 165 170 175 180 185

Q (U.S. gpm)

H (f

t)

0

40

50

60

70

80

10

20

30

90

100

110

120

Q (U.S. gpm)

P (h

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20

468

1012

Q (U.S. gpm)

NP

SH

(ft)

125 135 145130 140 150 155 160 165 170 175 180 185

125 135 145130 140 150 155 160 165 170 175 180 185

GRAPH 1

GRAPH 2

GRAPH 3



47

0

50

100

150

200

250

300

350

400

450

500

550

600

650

61

62

63

64

65

66

67

68

Q (U.S. gpm)

H (f

t)

61

62

63

64

65

66

67

68

0

15

10

5

20

25

30

35

40

Q (U.S. gpm)

P (h

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0

1

2

3

4

Q (U.S. gpm)

NP

SH

(ft)

70 75 80 85 90 95 100 105 110 115 120 125

70 75 80 85 90 95 100 105 110 115 120 125

70 75 80 85 90 95 100 105 110 115 120 125

GRAPH 1

GRAPH 2

GRAPH 3



48

SC (Sealed) Model

Part Description 1 2 3 4 5

Suction Casing Ductile Iron Ductile Iron 316 Stainless Cast Iron Cast Iron

Discharge Casing Ductile Iron Ductile Iron 316 Stainless Cast Iron Cast Iron

Stage Casing Ductile Iron Ductile Iron 316 Stainless Cast Iron Cast Iron

Side Channel Casing Ductile Iron Ductile Iron 316 Stainless Cast Iron Cast Iron

Foot Cast Iron Cast Iron Cast Iron Cast Iron Cast Iron

Shaft Steel Steel 316 Stainless Steel Steel

Impeller Bronze Steel 316 Stainless Bronze Steel

Suction Impeller Bronze Steel 316 Stainless Bronze Steel

Bearing Housing Cast Iron Cast Iron Cast Iron Cast Iron Cast Iron

Gasket Teflon Teflon Teflon Teflon Teflon

Sleeve Bearing Bronze (Carbon Option) Carbon Carbon Bronze (Carbon Option) Carbon

Additional Parts for SCM (Mag Drive) Model

Sleeve Bearing Stainless Stainless Stainless Stainless Stainless(Magnetic Coupling) Reinforced SiC Reinforced SiC Reinforced SiC Reinforced SiC Reinforced SiC

Shaft Sleeve SiC SiC SiC SiC SiC

Separation Canister 316 Stainless 316 Stainless 316 Stainless 316 Stainless 316 Stainless(Hastelloy Option) (Hastelloy Option) (Hastelloy Option) (Hastelloy Option) (Hastelloy Option)

The last number in your complete side channel model number is the material code. Please find material specification tables below accordingto these codes.

SiC = Silicon Carbide

MATERIAL SPECIFICATIONS


Basic ModelThis is the number at which you should have arrived through the sizing exercise.

Flange and PortsOptions: A - 300 Lb. ANSI compatible flanges / NPT tapped gauge and drain ports. (available for all models except 10 series)

D- DIN flanges / straight thread gauge portsW- DIN flange with weld neck compatible flanges included with the pump / NPT tapped gauge and drain ports

(available for 10 series only)

Sleeve Bearing MaterialOptions: B- Bronze (Available for all models except 60 series) (Only available in pumps with bronze impellers)

C- Carbon (All models)

Temperature OptionOptions 2- Standard for temperatures below 250°F (120°C).

3- Option for temperatures between 250°F (120°C) and 430°F (220°C). Also can be used as heating option for low temperature applications.Note: This option requires cooling water be supplied to pump.

Seal Type (see page 3-36 for guidance)A- Single Unbalanced (Discharge pressure from pump must be less than 230 psig (16 bar))B- Single Balanced (Good for pressures exceeding 230 psig (16 bar))C- Double Unbalanced (Discharge pressure from pump must be less than 230 psig (16 bar)) D- Double Balanced (Good for pressures exceeding 230 psig (16 bar))E- Quench Unbalanced (Discharge pressure from pump must be less than 230 psig (16 bar))G- Quench Balanced (Good for pressures exceeding 230 psig (16 bar))

O-ring MaterialB- NeopreneD- VitonE- TeflonG- Ethylene Propylene

Seal Face / Seal Seat1- Carbon Graphite / Aluminum Oxide (Standard for unbalanced single seals and all double seals)2- Aluminum Oxide / Carbon Graphite (Standard for single balanced seals)3- Silicon Carbide / Carbon Graphite (Standard for high temp option)4- Silicon Carbide / Silicon Carbide1L- Silicon Carbide / Carbon Graphite (Unbalanced single seal - LPG only) (Pressures below 230 psig (16 bar))2L- Carbon Graphite / Silicon Carbide (Balanced single seal - LPG only) (Pressures below 580 psig)3L- Carbon Graphite / Silicon Carbide (Balanced single seal - LPG only) (Pressures below 360 psig)

Material- Case / Impeller1- Ductile Iron / Bronze2- Ductile Iron / Steel3- Stainless Steel / Stainless Steel4- Cast Iron / Bronze5- Cast Iron / Steel

1

25 A C 2 B D 2 4

1 2 3 4 5 6 7 8

2

3

4

5

6

7

8

SC

49

MODEL NUMBER SELECTION GUIDE FOR MECHANICAL SEAL MODEL


50

26 A C 2 S2 G V 24 3

1 2 3 4 5 6 7 8 9

Basic ModelThis is the number at which you should have arrived through the sizing exercise.

Flange and PortsOptions: A - 300 Lb. ANSI compatible flanges / NPT tapped gauge and drain ports. (available for all models except 10 series)

D- DIN flanges / straight thread gauge portsW- DIN flange with weld neck compatible flanges included with the pump / NPT tapped gauge and drain ports

(available for 10 series only)

Sleeve Bearing MaterialOptions: B- Bronze (Only available in pumps with bronze impellers)

C- Carbon (All models)

Temperature OptionOptions 2- Standard for temperatures below 250°F (120°C).

3- Option for temperatures between 250°F (120°C) and 390°F (200°C). Also can be used as heating option for low temperature applications.

Bearing Material (Magnetic Coupling)S2- Silicon Carbide (Pressureless Sintered)

Ball Bearing LubricationO- OilG- Grease (Std)

Separation Canister MaterialV- Stainless SteelH- Hastelloy

Magnetic Coupling Size12- 1.1 Hp (10-30 Series)14- 2.6 Hp (10-30 Series)16- 3.8 Hp (10-30 Series)22- 2.6 Hp (20-50 Series)24- 7.6 Hp (20-50 Series)26- 11.3 Hp (20-50 Series)36- 16.8 Hp (40-50 Series)38- 28.5 Hp (40-50 Series)

Material- Case / Impeller1- Ductile Iron / Bronze2- Ductile Iron / Steel3- Stainless Steel / Stainless Steel4- Cast Iron / Bronze5- Cast Iron / Steel

1

2

3

4

5

6

7

8

SCM

9

MODEL NUMBER SELECTION GUIDE FOR MAGNETIC DRIVE MODEL


A Inlet(300 lb. ANSI Flanges)

B Outlet(300 lb. ANSI Flanges)

(SC10 series only)

SC10 series will be equipped withweld neck companion flanges on inlet and outlet.

1.9" (48.3 mm)

1.7" (43.2 mm)

N

O

P

M

Q

L

K

FE

G

J

D

H

C

51

NOTE: PUMP TURNS COUNTER-CLOCKWISE WHEN VIEWED FROMTHE DRIVE END.

SC–PUMP OUTLINE DIMENSIONS


Series Inlet OutletA* B* D E F G J K L M N O P

SC10 1-1/2 3/4 0.396.73 3.943.94 5.514.134.45 5.91 0.5140 20 10171 100100 1401051131425 150 135

SC20and 30

2-1/2 1-1/4 0.517.91 4.415.20 6.695.315.28 7.28 0.5565 32 13210 112132 1701351341940 185 146

SC40 3 1-1/2 0.597.68 5.205.51 7.686.105.59 7.87 0.5980 40 15195 132140 1951551422445 200 158

SC50 4 2 0.719.33 6.306.50 8.466.696.26 9.25 0.59100 50 18237 160165 2151701592850 235 1510

SC60 4 2-1/2 0.7910.31 7.097.09 9.657.686.77 9.25 0.59100 65 20262 180180 2451951723265 235 1510

1 Stage 2 Stage 3 Stage 4 Stage 5 Stage 6 Stage 7 Stage 8 StageSeries C H C H C H C H C H C H C H C H

SC10 7.68 8.03 9.02 9.37 10.35 14.65 11.69 12.05 13.03 13.39 14.37 14.72 15.71 16.06 17.05 17.40195 204 229 238 263 372 297 306 331 340 365 374 399 408 433 442

SC20and 30

8.39 8.94 9.96 10.51 11.54 12.09 13.11 13.66 14.69 15.24 16.26 16.81 17.83 18.39 19.41 19.96213 227 253 267 293 307 333 347 373 387 413 427 453 467 493 507

SC40 10.55 10.20 12.72 12.36 14.88 14.53 17.05 16.69 19.21 18.86 21.38 21.02 23.54 23.19 26.89 25.35268 259 323 314 378 369 433 424 488 479 543 534 598 589 653 644

SC50 12.01 12.32 14.96 15.28 17.91 18.23 20.87 21.18 23.82 24.13 26.77 27.09 29.72 30.04 32.68 32.99305 313 380 388 455 463 530 538 605 613 680 688 755 763 830 838

SC60 13.31 13.90 16.85 17.44 20.39 20.98 23.94 24.53 27.48 28.07 31.02 31.61 34.57 35.16 38.11 38.70338 353 428 443 518 533 608 623 698 713 788 803 878 893 968 983

* Inlet and outlet flanges are per DIN spec (PN40 DIN 2501). Flanges can be drilled per ANSI for 300 lb. flanges, except for SC10 series.**These dimensions are available in metric only. U.S. couplings must be machined before use.

Dimensions shown in grey area are millimeters while non-shaded areas are inches.

****

****

****

****

****

**

**

**

**

**

Q

Dimensions for Extra Foot on SCM Series Pumps (for stages 4-8 only)Pumps SCM10 SCM20 SCM30 SCM40 SCM50

Coupling sizes 12,14,16 12,14,16 12,14,16 22,24,26 22,24,26 Dimension 22,24,26 22,24,26 36,38 36,38

Q6.69 7.87 7.87 7.87 7.87170 200 200 200 200

R5.51 6.69 6.69 6.69 6.69140 170 170 170 170

S1.81 0.79 0.79 1.81 1.8130 20 20 30 30

T0.51 0.51 0.51 0.59 0.5913 13 13 15 15

52

BOutlet

AInlet

H

1.97" (50 mm)

1.10" (28 mm)

0.39" (10 mm)

4.13"(105 mm)

0.31" (8 mm)

0.55"(14 mm)

4.33"(110 mm)

2.17" (55 mm)

5.51"(140 mm)

C D

MLK

N

J

E

F

G

Q R

S

P

T

NOTE: 1) SCM10 series will be equipped with weldneck companion flanges on inlet and outlet. 2) For pumps containing four to eightstages, a middle foot is required. Fordimensions see the chart on page 34.

Inlet InletSeriesA1 B1 D2 E F G H J K L M N P2

SCM10 1.5 0.75 14.33 5.91 3.94 3.94 1.93 0.39 0.51 4.13 5.51 1.73 11.5440 20 364 150 100 100 49 10 13 105 140 44 293

SCM20 2.5 1.25 13.97 / 14.76 7.28 5.20 4.41 2.09 0.51 0.55 5.31 6.69 1.89 11.85 / 12.64and 30 65 32 355 / 375 185 132 112 53 13 14 135 170 48 301 / 321

SCM40 3 15 14.09 / 15.16 7.87 5.51 5.20 2.48 0.59 0.59 6.10 7.68 2.17 11.10 / 12.1780 40 358 / 385 200 140 132 63 15 15 155 195 55 282 / 309

SCM504 2 14.56 / 15.35 9.25 6.50 6.30 2.83 0.63 0.59 6.89 8.66 2.13 11.54 / 12.44

100 50 370 / 390 235 165 160 72 16 15 175 220 54 296 / 316

1Inlet and outlet flanges are per DIN spec (PN40 DIN 2501). Flanges can be drilled per ANSI for 300 lb flanges, except for SC10 series.2Depends on the magnetic coupling selected.

1 2 3 4 5 6 7 8

SCM10 7.68 9.02 10.35 11.69 13.03 14.37 15.71 17.05195 229 263 297 331 365 399 433

SCM20 & 30 8.39 9.96 11.54 13.11 14.69 16.26 17.83 19.41213 253 293 333 373 413 453 493

SCM40 10.55 12.72 14.88 17.05 19.21 21.38 23.54 25.71268 323 378 433 488 543 598 653

SCM50 12.01 14.96 17.91 20.87 23.82 26.77 29.72 32.68305 380 455 530 605 680 755 830

Series

CNumber of stages

SCM–PUMP OUTLINE DIMENSIONS


Dimensions shown in grey area are millimeters while non-shaded areas are inches.

53

Of the many hundreds of pump manufacturers in the United States,only a handful recommend their equipment for transferring liquefiedgases. There are various reasons for this, but the basic problem hasto do with the nature of a liquefied gas. The specific peculiarity ofa liquefied gas is that a liquefied gas is normally stored at its boilingpoint ... exactly at its boiling point! This means that any reduction inpressure, regardless of how slight, or any increase in temperature, nomatter how small, causes the liquid to start to boil. If either of thesethings happen in the inlet piping coming to the pump, the pumpperformance is severely affected. Pump capacity can be drasticallyreduced, the pump can be subjected to severe wear and themechanical seal and the pump may run completely dry, causingdangerous wear and leakage.

Although we cannot change the nature of the liquefied gas, there aremany things we can and must do to design an acceptable liquefiedgas pumping system.

Many of these design hints are incorporated in the accompanyingillustrations. You will note that each drawing is over-simplified and

illustrates just one principle. Normal fittings, strainers, unions, flexlines, valves, etc. have been ignored so that just that portion of thepiping which applies to the problem is shown. Do not pipe a plantfrom these incomplete illustrations! You should also note that all ofthese rules can be violated to a degree and still have a workablepumping system. You may see several places where your plant is atvariance from some of these. However, you should be aware thatevery violation is reducing your pumping efficiency and increasingyour pump maintenance cost. The principles apply to all makes andstyles of liquefied gas pumps ... rotary positive displacement,regenerative turbine or even centrifugal types.

This booklet is used in Corken Training Schools. Corken cooperateswith gas marketers, trade associations and other groups to conductcomplete training schools for persons involved in the transfer ofliquefied gases. These presentations include product information,safety, plant design and servicing equipment. Other information isavailable in various sections of the Corken catalog.

Warning: (1) Periodic inspection and maintenance of Corken products is essential. (2) Inspection, maintenance and installation of Corken products must be made only byexperienced, trained and qualified personnel. (3) Maintenance, use and installation of Corken products must comply with Corken instructions, applicable laws and safetystandards (such as NFPA Pamphlet 58 for LP-Gas and ANSI K61. 1-1972 for Anhydrous Ammonia). (4) Transfer of toxic, dangerous, flammable or explosive substancesusing Corken products is at user’s risk and equipment should be operated only by qualified personnel according to applicable laws and safety standards.

THE APPLICATION OF PUMPS TO LIQUEFIED GAS TRANSFER

PIPING RECOMMENDATIONS


54

3

1

5 6

10D

D

2

4

No!

Do not use restricted inlet line!

Yes!

Use inlet line larger than pumpsuction nozzle. Same size asnozzle OK on short runs.

No!

An eccentric reducer should always be used when reducing into any pump inlet where vapor might beencountered in the pumpage. The flat upper portion of the reducer prevents an accumulation of vapor that could interfere with pumping action.

Pressure drop caused by restriction in suction line will cause vaporization and cavitation.

Turbulence caused by flow interference close to the pump accentuates incipiant cavitation.

Yes!

No!

Concentric Reducer.

Do not locate restrictive fittingsor elbows close to pump inlet.

Yes!

Eccentric Reducer.

Best rule is 10 pipe diametersstraight pipe upstream frompump! (not always possible)



55

Locate pump close to tank!Directly under is best.Do not place pump far from tank!

Vaporization in the pump inlet line can displace liquid in the pump so that pump may start up in a dry condtition.A slope back toward the tank of only an inch or two in a 10 foot run will allow vapor to gravitate back into the tankand be replaced with liquid.

Low spots in bypass line can collect liquid which prevents normal vapor passage for priming purposes just likethe P trap in the drain of a kitchen sink. This is not a problem for bypass lines where vapor elimination is not required.

When possible, it is best to allow the pump to be fed by gravity flow to give stable, trouble-free operation.

8

11 12No! Yes!

Yes!

Keep return line level or go up toward tank!

No!

Do not slope liquid line up toward pump!

10

Yes!

Slight slope down toward pump is best.Perfectly level is OK.

Do not allow bypassline to have low spot.

9

7



56

Always locate pump below tank level... the lower the better!

Try not to locatepump abovelevel of liquidfeeding pump.Product mustbe able to flowby gravity intopump.

Low capacity flow through large lines often does not sweep out vapor. Flow occurs like liquid in a flume.Drawings 15 and 16 would allow vapor slugs to be drawn into the small pump causing erratic performance.Drawing 17 shows the best chance for stable feed into a small pump from a large line.

Since liquefied gases boil when drawn into a pump by its own suction, the pump must be fed by gravity flow togive stable, trouble-free operation.

7 14

16

17 18

No!

No!

No!

Yes!

Feeding small pump from tee off oflarge supply line. Come out thebottom of pipe line, not top or side!

When feeding smallpump from large main line, do not tee off theside. Tee out the bottom.

Yes!

When feeding smallpump from largemain line, do not teeoff the side.Tee outthe bottom!

Main Line

15

Vapor Liquid

Some tanks have vapor connections in the bottom. These have stand pipes inside. A bottom vapor connection can be used instead of a top opening with any of the drawings in this booklet.

13



57

No! Yes!

19 20

Better...

21

No underground liquefied gas pumpingsystem is good. Where tank must be buried,use one size smaller dip tube pipe, shallowtank, keep suction line short and use onlyCorken B166 bypass valve.

Bad...22

Tank too deep. Line too long. Suction pipe too large. Plan on higher pump maintenance and repair costs on all underground pumping systems.

23

No!Long Discharge Line

Back Check Valve

Large quantity of liquid in long lines allows continuingvaporization over long periods of time during whichthe pump will be full of vapor and will run dry duringstart-up attemps.

Use soft-seat back check valve near pump in longdischarge lines to prevent vaporization fromcoming back through pump when pumpis not in operation.

24

Yes!

Positive closure of back checkvalve prevents proper vapor return

for pump priming.

Back Check VavleExcess Flow Check Valve

Necessary for proper vapor eliminatiion when using priming type bypass valves.



Multiple pumps fedfrom same main line.

Pumps operatingin parallel.

Inquire about Corken’s Duplex-Series Pump Set.

25 26

28

29 30

Good... OK...

Parallel piping ofliquefied gas pumps.

27

Best... Bad...

No!Do not pipe bypass line back into suction piping! Heat buildup in recirculated products causes flashing of liquid to vapor with immediate cavitation and ultimate dry-running. This is why the bypass relief valves which are built into many positive displacement pumps should not be used for normal bypass action when handling liquefied gases. The internal valve should be considered to be a back-up safety relief in addition to a back-up safety relief in addition to a back-up safety relief in addition to a back-to-tank bypass valve and should be set to relieve at a pressure 10 to 20 psi higher than the working bypass. Some built-in bypass valves have the capability of being piped back-to-tank so check with the pump manufacturer.

Yes!Always pipe bypass back to tank! Make sure bypass line is large enough to handle full pump flow without excessive pressure build-up. Note that bypass line must be capable of bypassing full pump capacity without excessive pressure build-up. High pressure rise can cause bypass valve to chatter and vibrate.

Pump No. 1 is starved because of venturi action at

tee. This would be acceptable for

installations where both pumps would never operate at the same time.

58



Back check must be located to allow back-flowinto tank from vaporizer.

Back check must be located to allow back-flow intotank from vaporizer.

32

35

No!

Better... Best

No!

Back check valveprotects pump butallows back flowthrough bypass valve into storage tank. Use back checkwithout spring loaded valve to allow normalvapor elimination.

34

For pump capacities under 100 GPM, use abypass valve with built-in vapor elimination wherepossible. Like Corken's B166 or T166 valves.

Corken B166 Bypass Valve Functions.

33

31

To Vaporizer To Vaporizer

To Vaporizer

A B

Delivery line shut-off or pressure build up is so high that valve opens and relieves capacity back into supply tank.

Liquid from supply tank seeking its level in pump and bypass piping.

No circulation - all pump capacity going to delivery.

INLET INLET INLET

OUTLETOUTLETOUTLET

FIG. 1Relieving Operation

OPEN

FIG. 2Pumping Operation

CLOSED

FIG. 3Priming Operation

OPEN

36

Where A is a constant pressure bypass control valve and B is Corken B166 bypass and vapor elimination valve. Valve A is a fixed pressure bypass like the Fisher 98H which limits the feed pressure into the vaporizer to a specific value regardless of system vapor pressure. A differential difference in pressure exists between the pump discharge and the tank. Differential valve B must be set to the maximum acceptable differential of the pump while fixed pressure valve A is set for the vaporizer pressure requirement.

Some bypass valves, like the Corken B177,require tank pressure sensing lines. Checkinstructions for your valve.

59



60

INSTALLATION OF B166 VALVE

Proper installation of the Corken B166 valve will ensure optimumperformance of the pump as well as the valve. Install your B166valve on the discharge side of the pump, either vertically orhorizontally. All Corken Coro-Flo® turbine pumps have a 3/4" NPTopening in the discharge nozzle for piping this valve. For otherpumps a tee in the discharge line must be provided. The dischargepiping from the valve must go to the vapor section of the supply tankinto an excess flow valve, not a back check valve. The typicalinstallation is shown in Figure 2. The recommended valve dischargepipe line sizes are given in the table below. For distances of 50 ft. ormore, the next larger pipe size should be used.

Recommended Valve Discharge Line Sizes

ADJUSTMENT OFCORKEN B166 VALVE

The proper setting of the valve must be made at the time ofinstallation. Start the pump and circulate liquid through the valveback to the tank. Turn the valve adjusting screw out(counterclockwise) to decrease the pressure and in (clockwise) toincrease the pump discharge pressure.

Adjust the valve to open at the maximum pump pressure required tofill all containers.

Tighten the lock nut and permit the pump to circulate liquid throughthe valve. On stationary applications, if the motor overloadprotection device stops the motor, readjust the valve by turning thescrew out another turn or two.

Once a satisfactory pressure adjustment has been made, attach the"tamper-proof" seal furnished with your valve to preventunauthorized valve adjustment. On installations where the pump hasan internal safety relief valve, the B166 bypass valve should be setat a pressure slightly lower than the pump internal safety relief valve.

Your new Corken B166 valve (Figure 1) is a patented, dual purposeautomatic priming and differential bypass valve especially designedfor high pressure volatile liquid service, but it is suitable also as abypass valve for handling stable liquids. The B166 valve wasdeveloped for use with the Corken Coro-Flo® turbine regenerativepumps to keep the pump primed at all times and to act as adifferential bypass when needed. The B166 is also ideal forcentrifugal and other pumps.

AdjustingScrew

Socket HeadScrew

Locknut

Bonnet

Spring Seal

O-ring

Relief Spring

Discharge Line

O-ring

Ball Spring

BallBody

Valve

Flow Rate B166 Valve SizeGPM 3/4" 1"

Up to 20 3/4" 3/4"Up to 40 1" 1"

Figure 1

Figure 2

THE CORKEN B166 BYPASS VALVE


61

Adjusting ScrewLocknut

Bonnet

Spring Seal

O-ring

Relief Spring

O-ring

Socket HeadScrew

Body

Valve

INSTALLATION OF T166 VALVE

Proper installation of the Corken T166 valve will ensure optimumperformance of the pump as well as the valve. Install your T166valve on the discharge side of the pump, either vertically orhorizontally. The discharge piping from the valve should go to thevapor section of the truck tank into a filler type valve or a back checkvalve. A typical truck installation is shown in Figure 4. When thevalve is being used for vapor venting on stationary applicationsusing pumps with internal safety relief valves, the piping should bethe same as that used for the Corken B166. The recommended valvedischarge pipe line sizes are given in the table below. For distancesof 50 ft. or more, the next larger pipe size should be used.

Recommended Valve Discharge Line Sizes

ADJUSTMENT OFCORKEN T166 VALVE

The proper setting of the valve must be made at the time ofinstallation. Start the pump and circulate liquid through the valveback to the tank. Turn the valve adjusting screw out(counterclockwise) to decrease the pressure and in (clockwise) toincrease the pump discharge pressure.

Adjust the valve to open at the maximum pump pressure required tofill all containers. This is typically around 100 psi differential.

Tighten the lock nut and permit the pump to circulate liquid throughthe valve. On stationary applications, if the motor overloadprotection device stops the motor, readjust the valve by turning thescrew out another turn or two.

Once a satisfactory pressure adjustment has been made, attach the"tamper-proof" seal furnished with your valve to preventunauthorized valve adjustment. On installations where the pump hasan internal safety relief valve, the T166 bypass valve should be setat a pressure slightly lower than the pump internal safety relief valve.

Your new Corken T166 valve (Figure 3) has been especially designedfor use with delivery truck pumps to control the pump discharge pressureand to bypass excess liquid back to the truck tank. It is also quitesatisfactory for service with any positive displacement pump within itscapacity range and has been used in many stationary installations.

Flow Rate T166 Valve SizeGPM 1-1/4" 1-1/2"

Up to 40 1-1/2" 1-1/2"

Figure 3

Figure 4

THE CORKEN T166 BYPASS VALVE


62

Warranty Information

ONE YEAR LIMITED WARRANTYCorken, INC. warrants that its products will be free from defects in material andworkmanship for a period of 12 months following date of purchase from Corken.

Corken products which fail within the warranty period due to defects in material orworkmanship will be repaired or replaced at Corken's option, when returned, freightprepaid to Corken, INC., 3805 N.W. 36th St., Oklahoma City, Oklahoma 73112.

Parts subject to wear or abuse, such as mechanical seals, blades, piston rings, valvesand packing, and other parts showing signs of abuse, neglect or failure to be properlymaintained are not covered by this limited warranty. Also, equipment, parts andaccessories not manufactured by Corken but furnished with Corken products are notcovered by this limited warranty and the purchaser must look to the originalmanufacturer's warranty, if any. This limited warranty is void if the Corken producthas been altered or repaired without the consent of Corken.

All implied warranties, including any implied warranty of merchantability or fitnessfor a particular purpose, are expressly negated to the extent permitted by law andshall in no event extend beyond the expressed warrantee period.

Corken DISCLAIMS ANY LIABILITY FOR CONSEQUENTIAL DAMAGESDUE TO BREACH OF ANY WRITTEN OR IMPLIED WARRANTY ON CorkenPRODUCTS. Transfer of toxic, dangerous, flammable or explosive substancesusing Corken PRODUCTS is at the user's risk. Such substances should be handledby experienced, trained personnel in compliance with governmental and industrialsafety standards

PRICESAll prices are f.o.b. factory at Oklahoma City U.S.A. Prices quoted are foracceptance within 30 days, but in the meantime may be changed upon proper notice.Prices of equipment for future delivery will be those in effect at time of shipment.

TERMSStandard terms for all sales are net payment within thirty (30) days from the date ofinvoice unless it is the judgment of Corken that the financial condition of thepurchaser warrants other terms. In the event the purchaser fails to make paymentin accordance with the conditions specified, the purchaser shall pay interest on theamount due at the rate of 1.5 percent per month.

DESIGNIt is Corken's intention to continually improve the design and performance of itsproducts as new ideas, new practices and new materials become available.Therefore, all published designs, specifications and prices are subject to minormodifications at the time of manufacture to coincide with this policy, without priornotice to the purchaser. If the equipment purchased is to be used in an existinginstallation to match previously purchased equipment, material will be furnished tobe interchangeable as near as may be feasible, but Corken reserves the right tosubstitute materials and designs.

SHIPMENTSThe prices shown include standard crating or packaging for normal rail orcommercial truck shipments within the borders of the continental United States,Canada and Mexico. Consult factory for export crating charges. All promises ofshipment are estimates contingent upon strikes, fires, elements beyond our controlor manufacturing difficulties, including the scheduled shipping dates of materialsfrom our suppliers.

CANCELLATION CHARGESThere will be a minimum cancellation charge of 15 percent of the net price for anyorder which is cancelled after having been accepted and officially acknowledged byCorken. In the event there is material involved that is manufactured by others, andis being purchased by Corken for the sole purpose of becoming part of this canceledorder, the cancellation charges assessed Corken by these other manufacturers shallbe borne by the purchaser.

If shipment has already been made before notice of cancellation, the purchaser willbe charged all the freight costs involved in the handling of the order, including thecharges necessary to get the equipment back to the respective warehouses of Corkenand its suppliers, in addition to the cancellation charge described above.

RETURNED MATERIALMaterial may be returned to the factory ONLY if there is prior written authorizationfrom Corken and accompanied by a Corken CSC number and the freight is paid bythe shipper.

Material that is authorized for return will be inspected when received, and if it is ofcurrent design, unused, and in first-class resalable condition, credit will be allowedon the basis of the original invoice value less restocking charges. Returned materialthat is found to be worn, or in damaged condition, will not be accepted. Thecustomer will be notified of this, and return shipping instructions, or permission toscrap such items will be requested. If no instructions are received within sixty (60)days after such notice, the material will be scrapped. Outside purchased materialsand equipment may be returned for credit ONLY by Corken's prior writtenauthorization, and must be in new and undamaged resalable condition, and ofcurrent design. Such returned materials are subject to a MINIMUM restockingcharge of 25 percent.

LITERATURECorken will furnish, upon request and without charge to the purchaser, six copiesof paper prints of standard drawings, performance curves, and other currentliterature covering the pump or compressor and/or such other descriptive materialthat good judgment would consider necessary. Any additional material and/orspecial drawings will be charged for at appropriate rates determined by Corken. SeeCorken optional services in price pages for details.

FACTORY INSPECTION AND TESTSEach article of Corken's manufacture passes a standard factory inspection andoperating test prior to shipment. Special factory inspections, tests and/or certifiedtest reports are all subject to a factory charge available upon request.

LIABILITY FROM USE OF PRODUCTCorken has no control over the ultimate use of its products and specifically disclaimsany liability damage, loss or fines which may arise from the use thereof. The userand purchaser shall hold Corken harmless from such damage, loss or fines. Theuser and purchaser shall determine the suitability of Corken products for the useintended and issue adequate safety instructions therefore.

Compliance with the Occupational Safety and Health Act and similar laws andregulations shall be the responsibility of the user of the product and not theresponsibility of Corken.

63

NOTE: Gallon - designates to the U.S. gallon. To convert into the Imperial gallon, multiplythe U.S. gallon by 0.83267.

Bar 33.456 Feet H2O @ 39°FBar 29.530 In. Hg @ 32°FBar 1.0197 kg/cm2

Bar 14.504 Pounds/in2

Centimeters 0.3937 InchesCentimeters 0.01 MetersCentimeters 10 MillimetersCentipoise 0.001 Pascal - secondCentipoise 0.01 PoiseCentistokes 0.01 Sq. cm / sec.Centistokes 0.01 StokesFeet 30.48 CentimetersFeet 0.166667 FathomsFeet 3.0480 x 10-4 KilometersFeet 304.8 MillimetersFeet 12 InchesFeet 0.3048 MetersFeet 1/3 YardsFeet of water 0.0295 AtmospheresFeet of water 0.8826 Inches of mercuryFeet of water 304.8 Kgs. / sq. meterFeet of water 62.43 Lbs. / sq. ft.Feet of water 0.4335 Lbs. / sq. inchGallons 3785 Cubic centimetersGallons 0.1337 Cubic feetGallons 231 Cubic inchesGallons 3.785 x 10-3 Cubic metersGallons 4.951 x 10-3 Cubic yardsGallons 3.785 LitersGallons 8 Pints (liq.)Gallons 4 Quarts (liq.)Gallons - Imperial 1.20095 U.S. gallonsGallons - U.S. 0.83267 Imperial gallonsGallons / min. 2.228 x 10-3 Cubic feet / sec.

MULTIPLY BY TO OBTAIN

Conversion Factors

Company Name and Location

Submitted By: Date:

Phone Number: FAX Number:

COMPRESSOR

Gas: (if mixture, provide % breakdown)

Inlet Pressure: psig Outlet Pressure: psig

Inlet Temperature: °F

Volume (flow rate) (scfm, acfm, nm3/hr, m3/hr, etc.)

Duty Cycle: Continuous Intermittent

Atmospheric Pressure: psia

Oil Free Compression Required? Yes No

PUMP

Liquid: Specific Gravity:

Discharge Pressure: psig Inlet Temperature: °F

Differential Pressure: psig Viscosity:

Flow Rate: m3/hr, gal/ltr (per. minute) NPSHA:

Power Available: Phase Hz Voltage

APPLICATION SUMMARY

NOTES

End Use: End User:

Product Application Form

64

3805 N.W. 36th St., Oklahoma City, OK 73112Phone (405) 946-5576 • Fax (405) 948-7343

E-mail [email protected] address www.corken.com

CP370D PRINTED IN THE USA APRIL 2008

Documents

Corken Specialty Selection Guide Selective Catalytic ... · PDF fileCorken Specialty Selection Guide Selective Catalytic Reduction Systems • Anhydrous Ammonia • Aqueous Ammonia